WO2016195116A2 - Liquid processing nozzle, liquid processing method using same, gas dissolution method, and gas dissolution device - Google Patents

Abstract

Provided is a liquid processing nozzle that exhibits very efficient generation of microscopic bubbles and excellent gas dissolution capacity.　The liquid processing nozzle 1 is provided with: a nozzle body 2 having a liquid passage 3 formed therein; and a processing core CORE comprising protrusions 10 that protrude from the inner surface of the liquid passage 3 and that have, formed in the circumferential direction and on the outer peripheral surface thereof, a plurality of alternating contiguous ridge sections 11 and valley sections 12, the valley sections 12 serving as high flow rate sections. The effective valley point density (Ne/St) normalized by the entire flow cross-sectional area (St) is maintained at at least 1.5 parts/mm². For the protrusions 10, the effective valley point density (Ne/St), which is the number (Ne) of effective valley points normalized by the entire flow cross-sectional area (St), is maintained at at least 1.5 parts/mm².

Description

Liquid processing nozzle, liquid processing method, gas dissolving method and gas dissolving apparatus using the same

The present invention relates to a liquid processing nozzle, and more particularly to a liquid processing nozzle excellent in efficient generation of fine bubbles and gas dissolving ability, and also relates to a liquid processing method, a gas dissolving method and a gas dissolving apparatus realized using the nozzle. is there.

In recent years, fine bubbles called microbubbles (fine bubbles) or nanobubbles (ultra fine bubbles) have been applied to many applications, and various bubble generation mechanisms have been proposed. The two-phase flow swirl method disclosed in Patent Document 1 is intended to reduce the size by entraining the outside air into the swirl flow and forcibly pulverizing, and has a disadvantage that the generation efficiency of nanobubbles with a bubble diameter of less than 1 μm is poor. There is. On the other hand, a so-called cavitation method is used in which a throttle hole is provided in the water flow path by a venturi or an orifice, and the dissolved air is precipitated as fine bubbles by the pressure reducing effect resulting from Bernoulli's theorem when water passes at a high flow rate. Various microbubble generation mechanisms have been proposed (Patent Documents 2 to 10). In particular, in the methods disclosed in Patent Documents 6 to 10, a screw member is arranged in the middle of the throttle hole, and the water flow is further accelerated by a gap formed between the screw valleys or the opposing screw members. Thus, cavitation efficiency can be improved and nanobubbles can be generated at a higher density. In Patent Documents 6 and 7, it is shown by bubble measurement using a laser diffraction particle size meter or the like that bubbles in the nano region can be obtained with high density.
Further, when the water flow passes through the collision portion formed by the screw member, the water flow is vigorously stirred by the Karman vortex generated based on the flow detour and the reduced-pressure boiling phenomenon due to cavitation. Therefore, when a gas such as air or ozone is mixed with the water flow and supplied to the nozzle in a mixed phase state, the gas is caught in the strong stirring region formed by the screw member, and can be efficiently dissolved. In addition, the gas phase that could not be dissolved can be refined with a stirring flow and coexist with the dissolved gas in the form of nanobubbles. Such a gas dissolution method is disclosed in Patent Document 8 and Patent Document 9.

JP 2008-229516 A JP 2008-73432 A JP 2007-209509 A JP 2007-50341 A JP 2006-116518 A WO2010 / 055702 publication WO2013 / 012069 JP 2011-240206 A WO2013 / 011570

Although it is clear that the liquid processing nozzles disclosed in Patent Documents 6 to 10 are capable of generating fine bubbles from the measurement results of the disclosed laser diffraction particle size meter, the generation efficiency of the fine bubbles is not sufficient. There is a problem I can't say. For example, when the nozzles disclosed in these publications are actually incorporated into a shower and used for evaluation of the cleaning power and body feeling (especially the moisture retention properties of the hair) when washing the hair, the effect is not as high as expected. It turned out that there were many users who answered that there was a lack of moisture retention. In addition, a test was conducted in which gas such as carbon dioxide or oxygen was supplied to these nozzles together with water to dissolve the gas, but satisfactory results were not obtained with respect to the gas dissolution efficiency.
The above problem is considered to be caused by the fact that the conditions for generating cavitation that govern the generation of fine bubbles and gas dissolution performance of the nozzle are not optimized. However, there are many parameters that are considered to dominate the cavitation, such as the size of the screw to be used, the pitch and depth of the thread valley, the number and arrangement of the screws, the formation form of the gap, and the cross-sectional area of the flow path at the screw position. Since many trade-off parameters are included, it is almost hopeless to systematically improve bubble generation efficiency and gas dissolution efficiency only by trial and error design change of nozzle dimensions.
The above Patent Documents 6 to 9 only qualitatively disclose the principle of generation of fine bubbles, and the configuration examples of typical nozzles do not disclose any dimensional information on screws or nozzle bodies. Even if it is disclosed, there is only one point. In other words, almost nothing is disclosed as to which elements of the nozzle should be changed to optimize the generation efficiency of fine bubbles and gas dissolution efficiency, and as a result, how much performance It is impossible to grasp whether there is an improvement fee. In these documents, only the relative bubble diameter distribution of fine bubbles is disclosed in these documents, and the effect that is specifically obtained when water is used (for example, improvement of moisture retention such as hair) This is also related to the fact that no data is disclosed about the degree of gas dissolution, etc.), and it is impossible to grasp the quantitative trend between the amount of generated bubbles and the expected effect.
The problem of the present invention is that it has excellent cavitation ability and thus fine bubble generation ability, and also has a liquid treatment nozzle that clearly outperforms the prior art in terms of performance advantages such as improvement of moisture retention and gas dissolution ability of hair, An object of the present invention is to provide a liquid processing method, a gas dissolving method and a gas dissolving apparatus using the same.

In order to solve the above problems, the liquid processing nozzle of the present invention is:
A nozzle body in which a liquid channel having a liquid inlet at one end and a liquid outlet at the other end is formed;
A processing core portion having a collision portion formed so that a plurality of circumferential ridges and valleys that become high flow velocity portions are alternately connected to the outer peripheral surface while projecting from the inner surface of the liquid flow path,
In the projection onto the plane orthogonal to the central axis of the liquid flow path, the entire area inside the outer peripheral edge of the projection area of the liquid flow path in the processing core portion is S1, and the projected area area of the collision portion is S2. Distribution cross section St
St = S1-S2 (unit: mm ² )
When the cross-sectional area of the liquid inlet and the liquid outlet is set larger than the total flow cross-sectional area St,
The depth h of the valley appearing in the projected outline of the collision portion is secured to 0.2 mm or more, and the inner periphery of the liquid flow path centering on the projection point of the central axis among the valley points representing the bottom position of the valley portion N is the number of objects located inside the reference circle drawn with a radius equivalent to 70% of the distance to the distance, Nc is the number of objects located outside the reference circle, and the valley depth correction coefficient α
α = 1 when h ≧ 0.35 mm.
When h <0.35 mm, α = −60h ² + 41h-6 (1)
As
The area of the portion located inside the reference circle in the region of the total cross-sectional area in the projection is S ₇₀ (Unit: mm ² ) 70% section ratio σ ₇₀ The
σ = S ₇₀ / St x 100 (%)
The effective valley point number Ne is determined as
Ne = α · (0.38Nc ₇₀ + (Σ ₇₀ / 50) ・ N ₇₀ (2)
When defined as
Effective valley point density expressed by Ne / St is 1.5 / mm ² It is characterized by being secured above.
Further, the liquid processing method of the present invention is characterized in that a liquid is supplied to the liquid inlet of the liquid processing nozzle of the present invention, and the liquid is brought into contact with the collision portion and flows out from the liquid outlet.
According to the present invention, when the liquid flow in the nozzle body collides with the collision part and detours downstream thereof, the liquid flow is increased in speed by squeezing in the valley part to cause cavitation. Stir the liquid vigorously while In addition to this, a vortex generated when the high-speed flow bypasses the collision portion is added, and a very remarkable stirring region is formed in the vicinity of the collision portion and in the immediately downstream region. The decompression area where the bubbles are deposited is limited to the vicinity of the valley bottom around the collision part, and the high-speed liquid flow passes through the area almost instantaneously. It will be caught in and will generate fine bubbles. As described above, cavitation occurs mainly in the valleys of the collision part, and it is important to increase the generation efficiency of microbubbles by bringing at least one of these valleys into contact with the flow. Therefore, increasing the number of screw valleys arranged in the cross section of the processing core portion seems to be effective for improving the generation efficiency of cavitation and, in turn, fine bubbles. However, when the present inventors examined in detail, it turned out that a problem is not so simple and even if the number of troughs is increased mechanically, it does not simply lead to improvement in the generation efficiency of fine bubbles. The present inventors examined the factors by dividing them into the following items.
(1) If the formation interval of the valley part of the collision part is made constant, the cross-sectional dimension of the liquid channel in the processing core part is increased, and the protrusion height from the inner surface of the flow path of the collision part is increased. The number of valley points that exist increases. However, in this case, since the cross-sectional area of the flow path also increases and the flow rate increases with the same liquid supply pressure, the number of valleys allocated per unit flow rate does not necessarily increase, and in some cases, the flow rate per unit flow rate It is actually possible that the number of valleys will decrease and the cavitation efficiency will decrease instead. Therefore, it is not the absolute number of valley points formed in the processing core part, but the valley point density normalized by the channel cross-sectional area that dominates the cavitation efficiency and hence the fine bubble generation efficiency. This is also closely related to how many valley points the liquid per unit flow rate contacts.
(2) The flow velocity in the pipe line has a parabolic distribution in the radial direction in a form that becomes maximum near the center of the cross section of the pipe axis and becomes minimum at the position of the inner wall surface of the pipe. Therefore, the position of the valley in the cross section of the flow path does not contribute to the generation of fine bubbles equivalently, but the valley close to the center of the cross section is easier to secure the flow rate necessary for cavitation, Great contribution. Therefore, when evaluating the number of valley points, it is necessary to consider different weights depending on the distance from the center of the cross section.
(3) The valley point located near the cross-sectional center actually contributes effectively to the cavitation effect only when the expected flow velocity is obtained near the cross-sectional center. At first glance, this seems to be a trivial matter, but placing the valley near the center of the cross section means that a considerable part of the collision part that forms the valley occupies the central area of the cross section. As the number of valleys near the center of the cross section increases, the dilemma that the flow is hindered and the flow velocity cannot be secured increases. The flow obstructed by the obstacle in the central area of the cross section goes around the outer edge area of the cross section, and there is a possibility of contributing to the improvement of the flow velocity in the area where the flow rate tends to be insufficient, but the central area of the cross section is not obstructed. Compared to being able to pass through, significant flow loss is unavoidable. Therefore, the number of valley points arranged in the vicinity of the cross-sectional center needs to be evaluated by giving a weight to the distribution area near the cross-sectional center.
(4) If the formation interval of the valleys formed in the collision part is narrowed, the number of valleys can be increased even with the same flow path cross-sectional area. However, when the depth of the valley portion decreases with the formation interval of the valley portion, there is a concern that the flow restricting effect at the valley bottom is reduced, leading to a reduction in cavitation efficiency. Therefore, when adopting a collision portion having a small valley depth in order to secure a larger number of valley points, it is necessary to evaluate the number of valley points by weighting according to the valley depth.
The present inventors have made a number of liquid treatments in which the size of the collision part and the formation depth of the valley part, the number and arrangement of the collision parts, and the flow path cross-sectional dimensions in the processing core part where the collision parts are arranged are variously set. A nozzle was manufactured, and the concentration of fine bubbles, characteristics of the treated liquid containing fine bubbles, and gas dissolution efficiency were examined in detail. As a result, we arrived at a method that accurately weights the valley density of the collision part in the processing core part described in (1) above, reflecting the three factors (2) to (4). As a result, the inventors have found that there is a numerical range that is clearly superior to the liquid processing nozzle disclosed in the above-mentioned patent document in terms of the cavitation efficiency and thus the fine bubble generation efficiency. It is a thing.
Hereinafter, it demonstrates in order. First, as a premise, the cross-sectional areas of the liquid inlet and the liquid outlet are set larger than the total flow cross-sectional area St of the processing core part. This is because if the cross-sectional areas of the liquid inlet and the liquid outlet are smaller than St, the flow rate loss at the liquid inlet and the liquid outlet becomes too large, and a flow velocity for generating sufficient cavitation at the processing core can be secured. Because it disappears. More preferably, the cross-sectional areas of the liquid inlet and the liquid outlet are set to be larger than the entire area S1 inside the outer peripheral edge of the projection region of the liquid channel in the processing core. Moreover, as a liquid pressure in the case of distribute | circulating a liquid to a liquid processing nozzle, about 0.03 MPa to about 0.4 MPa is assumed centering on 0.1 MPa which is a standard water supply pressure.
As for the factor (2), a reference circle is set with a radius corresponding to 70% of the distance from the center axis projection point to the inner peripheral edge of the liquid channel. In the above-described liquid pressure range in the conduit having no obstacle, the ratio of the average flow velocity outside the reference circle to the flow velocity inside the reference circle is approximately 0.38: 1. Number of valleys on the outside Nc ₇₀ Is the number of valleys N inside the reference circle. ₇₀ It has been found that it is appropriate to weight such that the contribution is reduced to about 0.38 times the contribution of.
For factor (3), 70% section ratio σ ₇₀ = S ₇₀ The value of / St × 100 (%) is 50% if there is no collision part. Therefore, even when the collision part is arranged, the value of the 70% cross-section ratio becomes closer to 50% and becomes closer to the inner side of the reference circle. The trough will receive a higher flow velocity. Therefore, the number N of valleys inside the reference circle ₇₀ For σ ₇₀ We thought it appropriate to weight by the value of / 50.
Regarding the factor (4), as a result of various investigations on the influence of the depth of the valley, first, when the depth h of the valley that appears in the projected outline of the collision portion is less than 0.2 mm, fine bubbles It was found that the occurrence of is not expected. When the value of the depth h of the valley portion increases to 0.2 mm or more, the contribution to the generation of fine bubbles gradually increases as h increases, and the influence of the valley depth h on the generation of fine bubbles is expressed as h = 0. Experimental verification of fine bubble generation efficiency and gas dissolution efficiency when weighting is applied to the number of valley points at a ratio of 0.5: 0.9: 1.0 for each case of .25 mm, 0.3 mm, and 0.35 mm The inventors have found that the results can be well explained. It was also found that when the valley depth h is 0.35 mm or more, the effect of h reaches a peak. Therefore, as described above, the number N of valley points inside the weighted reference circle ₇₀ And the number of valleys Nc outside the reference circle ₇₀ As a weight for the sum of the above, the valley depth correction coefficient α is determined by the above equation (1). As described above, the quadratic expression of h according to the second expression of (1) is 0.5, 0.00 as the values of α when h is 0.25 mm, 0.3 mm to 0.35 mm, respectively. An empirical rule that 9 to 1.0 is appropriate is approximated by a quadratic equation, and h takes a value other than the above within a relatively narrow numerical range of 0.2 to 0.35 mm. In this case, an appropriate value of α can be reasonably calculated.
Thus, the number of valleys Ne weighted by the coefficients optimized for each of the three factors is as shown in the above-described equation (2). The effective valley point density Ne / St obtained by standardizing the effective valley point number Ne with the total flow cross-sectional area St of the processing core portion is an index for objectively quantifying the fine bubble generation capability of the liquid processing nozzle. . And the value is 1.5 / mm ² When the above is ensured, the cavitation efficiency and thus the generation efficiency of fine bubbles are clearly improved as compared with the liquid processing nozzle disclosed in the above-mentioned patent document, and various effects peculiar to liquids containing fine bubbles are manifested at an unprecedented level. It can be made. The effective valley point density is more desirably 1.8 pieces / mm. ² It is good to secure the above. The axial cross-sectional shape of the liquid channel is preferably circular, for example, but it should be formed as having an elliptical or regular polygonal (square, regular hexagon, regular octagon, etc.) axial cross section unless excessive loss occurs. Is also possible.
A plurality of ridges formed in the collision portion can be integrally formed in a spiral shape. In this way, the formation of the peak is facilitated, and the peak is inclined with respect to the flow, so that the flow component crossing the ridge line of the peak increases, and the turbulent flow generation effect accompanying flow separation becomes significant. Therefore, the bubbles can be further miniaturized. In this case, if the collision part is formed by a screw member whose leg end side protrudes into the flow path, the thread of the screw member can be used as a thread part, and the manufacturing is easy.
Although there is no limit to the upper limit of the effective valley point density in the processing core part, as described above, it is necessary to secure a valley depth of 0.20 mm or more from the viewpoint of ensuring cavitation efficiency, so it is realistic to increase it indefinitely. It is difficult to do. As for the depth of the valley portion, the flow throttling effect is saturated at 0.35 mm or more as described above, and the valley depth correction coefficient α is uniformly set to 1.0, so that the valley point density is increased. From the viewpoint, it is preferable that the upper limit of the depth of the valley portion is limited to about 0.4 mm slightly exceeding 0.35 mm. That is, the depth of the valley portion of the collision portion is preferably set to 0.20 mm or more and 0.40 mm or less, and more preferably 0.25 mm or more and 0.35 mm or less. In this case, the cross-sectional shape of the liquid flow path in the processing core portion is circular, and the effective valley point density Ne is 1.5 / mm. ² In order to ensure the above, the inner diameter D should be 2 mm or more and 7 mm or less (preferably 2 mm or more and 6 mm or less), and the total cross-sectional area St is 1.2 mm at this time. ² 35mm or more ² Below (desirably 1.2mm ² 20mm or more ² The following can be secured. When the outlet side of the liquid processing nozzle is opened and water is supplied to the inlet side at a liquid pressure of 0.1 MPa, the flow rate per one liquid flow path is approximately 0.5 L / min to 26 L / min (desirably Is 0.5 L / min or more and 15 L / min or less), and can form a wide flow spectrum suitable for various applications.
For example, when the collision part is formed of a screw member having a JIS coarse pitch, the collision part has an outer diameter M of 1.0 mm (the depth of the valley is 0.25 mm) or more and 2.0 mm (the depth of the valley is 0. 0). 40 mm) or less, and more preferably 1.4 mm (valley depth is 0.30 mm) or more and 1.6 mm (valley depth is 0.35 mm) or less.
As an arrangement form of the collision part in the liquid channel, for example, as one of the simplest ones, a form in which the cross section of the channel is bisected and arranged in the diameter direction can be exemplified. This configuration can increase the number of valleys inside the reference circle by, for example, not forming a gap in the vicinity of the center of the cross section or setting the gap interval to a small value even if it is formed. It has the geometric property that the point density decreases rapidly. Therefore, this configuration is effective when it is desired to improve the fine bubble generation efficiency of the liquid processing nozzle with a small flow rate. Specifically, the inner diameter D of the liquid channel is set to 2 mm to 4.5 mm (preferably 2 mm to 3.5 mm), and the total flow cross section St is 1.2 mm. ² 10 mm or more ² Below (desirably 1.2mm ² More than 5mm ² It is better to set it to the following), and the effective valley point density is 1.5 / mm. ² The above can be ensured and good fine bubble generation efficiency can be achieved. When the outlet side of the liquid treatment nozzle is opened and water is supplied to the inlet side at a liquid pressure of 0.1 MPa, the flow rate per one liquid flow path is approximately 0.5 L / min to 7.5 L / min. (Desirably 0.5L / min to 5L / min).
On the other hand, it is possible to arrange three or more collision parts in a form surrounding the central axis in projection, for example, four in a cross shape. In this configuration, there is an area where the arrangement of valley points is geometrically impossible near the center of the flow path cross section inside the reference circle due to the fact that the tip of the collision part gathers from three or more directions. By increasing the number of collision parts compared to the configuration of the previous paragraph, there is an advantage that the effective valley point density can be increased particularly in a configuration having a large channel cross-sectional area (that is, a configuration requiring a large flow rate). A set of cross-shaped collision portions respectively formed in the throttle holes can be easily formed by, for example, a plurality of screw members that are screwed so that the front ends protrude into the throttle holes from the wall outer peripheral surface side of the nozzle body. Other than 4, it is possible to select from 3, 5, 6, 7, and 8.
In the configuration in which four protrusions are arranged in a cross shape, specifically, the inner diameter D of the liquid flow path is set to 2.5 mm to 7 mm (preferably 2.9 mm to 5.5 mm), and the entire flow is interrupted. Area St 2.5mm ² 35mm or more ² Below (preferably 4mm ² More than 13mm ² Or less), and the effective valley point density is 1.5 / mm. ² The above can be ensured and good fine bubble generation efficiency can be achieved. When the outlet side of the liquid processing nozzle is opened and water is supplied to the inlet side at a liquid pressure of 0.1 MPa, the flow rate per one liquid flow path is approximately 2 L / min to 25 L / min (preferably 3 0.5 L / min to 13 L / min).
In this case, the liquid flow gap can be formed at the center position of the cross section where the tips of the plurality of collision portions gather. For example, when the liquid circulation gap is formed at the center position of the cross, the flow at the center of the cross section (center flow) at which the flow velocity is the highest is not easily obstructed by the formation of the liquid circulation gap. ₇₀ As a result, the number of effective valleys increases even with the same number of valleys, and the generation efficiency of fine bubbles is further improved. By forming this liquid flow gap, the 70% cross-sectional ratio σ ₇₀ It is easy to secure 40% or more. The above-mentioned effect due to the formation of the liquid flow gap is particularly remarkable when the front end surface forming the liquid flow gaps of the four collision parts is formed flat and the liquid flow gap is formed in a square shape in the above-described projection. is there.
When a plurality of collision parts are arranged in the liquid channel in the processing core part, it is also possible to arrange the plurality of collision parts at positions shifted from each other in the axial direction (flow direction) of the liquid channel. In this way, a plurality of collision parts can be provided in the flow direction, and the flow can be repeatedly brought into contact with the troughs serving as cavitation points, so that the generation efficiency of microbubbles and the gas dissolution efficiency described later can be improved. Contributes to improvement.
In the liquid processing nozzle of the present invention, a single liquid flow path formed in the nozzle body can be provided. In this case, when it is desired to increase the total flow rate of the liquid to be processed, a plurality of nozzles can be connected in parallel by a branch joint or the like. In this way, even if the flow rate per nozzle is small, the entire flow rate can be secured without sacrificing the cavitation effect.
On the other hand, a partition that partitions the liquid flow path into an inflow chamber on the liquid inlet side and an outflow chamber on the liquid outlet side, and a plurality of throttles that are formed through the partition and communicate with each other through different paths. It is also possible to form a collision part in a form that includes a hole and the processing core part protrudes from the inner surface of the throttle hole. In other words, when a plurality of nozzles are connected in parallel, the flow path before and after the processing core part where the collision part is arranged is arranged independently for each nozzle. The throttle section is formed, and the flow path sections before and after the throttle section are aggregated into an inflow chamber or an outflow chamber defined by the partition wall and shared by the plurality of throttle sections. As a result, the section where the flow path branches into a plurality of systems can be shortened only to the throttle hole formed in the partition wall, which contributes to the prevention of the occurrence of drift due to the length of the branch flow path.
In this case, the throttle hole has a diameter of a circle equivalent to the sum of the axial cross-sectional areas of the throttle holes, de and the length of the throttle hole is L, and the throttle hole aspect ratio defined by L / de is 3.5. In the projection onto a plane that is set as follows and is orthogonal to the axis of the nozzle body, the distance T from the reference point defined at the center position of the projection area of the partition wall to the inner periphery of the plurality of throttle holes is the throttle hole. It is preferable to arrange them close to each other so as to be smaller than the inner diameter D. If the thickness of the partition wall increases, the length of the throttle hole itself having a small cross-sectional area increases, and even if the sections before and after it are concentrated in the inflow chamber or the outflow chamber, drift may be likely to occur. In addition, when the plurality of throttle holes formed in the partition wall are formed in the outer peripheral region of the partition wall where the flow velocity is reduced by fluid friction with the inner wall of the tube, drift may easily occur due to the effect of the decrease in the flow velocity. . Therefore, by setting the throttle hole aspect ratio to 3.5 or less as described above, the length of the branch section that causes the drift, that is, the length of the throttle hole in which the collision portion is arranged is sufficiently shortened. Further, by arranging the throttle holes close to the reference point, the throttle holes are collected at the center of the partition wall portion where the flow velocity is high. In other words, all the throttle holes are gathered and arranged at a position close to the center of the partition wall. As a result, the reduction or non-uniformization of the flow velocity in the throttle hole is suppressed, and drift can be reliably prevented. The value of the aperture hole aspect ratio L / de is desirably 3 or less, and more desirably 2.5 or less. Further, the throttle hole displacement T is desirably 1/2 or less of the inner diameter D of the throttle hole.
In addition, from the viewpoint of suppressing flow loss in the throttle hole and preventing drift, the value of the throttle hole aspect ratio defined by L / de is a space required for arranging the collision portion. It can be said that it is desirable to set it as small as possible within the range that can be secured on the inner surface of the throttle hole (as will be described later, when the inner surfaces of the inflow chamber and the outflow chamber are tapered surfaces that are reduced in diameter toward the partition wall, There may be a configuration in which the tapered surface is directly connected and the collision portion is formed at the coupling position, but the length of the throttle hole in this case is defined as a value equal to the outer diameter at the protruding proximal end position of the collision portion). Also, the value of the throttle hole displacement T is preferably set as small as possible from the viewpoint of increasing the flow velocity in the throttle hole. For example, when the two throttle holes are formed in contact with each other at the central portion of the partition wall, the value is zero. Does not prevent becoming.
The throttle hole may be a hole having a uniform cross section in the flow axis direction or a hole having a non-uniform cross section that is reduced in diameter at the intermediate portion. In this specification, “the axial cross-sectional area of the throttle hole” means an axial cross-sectional area at a position where the value is the smallest in the flow axis direction. The plurality of throttle holes can have different axial cross-sectional areas, but in this case, the inner diameter D of the throttle hole means an average value for the plurality of throttle holes. The same applies to the length of the aperture. Furthermore, the center position of the projection area of the partition wall means the center when the projection area is circular. However, the projected area of the partition wall is allowed to be a regular polygonal shape or an elliptical shape from the concept of the invention. In this case, the geometric gravity center position of the projected area is determined as the center position.
Further, when the length of the section located downstream from the collision portion of the throttle hole (hereinafter referred to as the remaining section) is Lp, and the diameter of a circle equivalent to the sum of the axial sectional areas of the throttle holes is de, Lp / The remaining section aspect ratio defined by de is preferably set to 1.0 or less. Thereby, the passage distance of the remaining section of the throttle hole having a large fluid resistance of the flow including the precipitated bubbles is shortened until the liquid that has passed through the collision portion in the plurality of throttle holes merges in the outflow chamber, As a result, the strong stirring region generated downstream of the collision part of each throttle hole is also integrated in the outflow chamber, and the effect of miniaturizing the bubbles is further enhanced.
Further, with respect to the aperture hole, the requirement for the proximity arrangement near the center of the partition wall (around the reference point) can be further embodied as follows. That is, in the projection onto the plane orthogonal to the axis of the nozzle body, when St is the area of the circumscribed circle with respect to the inner periphery of the plurality of throttle holes and Sr is the total area of the projection areas of the throttle holes, K≡Sr / St The aperture hole aggregation rate K defined as follows is 0.2 or more. For example, in the case of a set of a plurality of throttle holes having the same size and the same number of formations, the circumscribed circle area increases as the throttle hole displacement T increases. Therefore, the throttle hole concentration ratio K can be a parameter representing the concentration degree of the throttle holes in the central region of the partition wall, and by setting the K to 0.2 or more, the drift suppression effect becomes more remarkable, and the generation of fine bubbles Contributes to further improvement in efficiency and gas dissolution efficiency.
The “circumscribed circle” is defined as a circle circumscribing all of the inner peripheral edges of the plurality of aperture holes (minimum diameter portions) in the projection. If the circle circumscribing the inner periphery of all the apertures cannot be drawn geometrically, “the largest circle that circumscribes the inner periphery of one or more apertures and does not intersect the inner periphery of the remaining apertures. ".
The area St of the circumscribed circle is desirably 90% or more of the projected area of the partition wall. Thereby, the area of the flow blocking region formed outside the throttle hole in the partition wall can be reduced, and the flow stagnation and the loss due to the vortex generated in these regions can be reduced. When the circumscribed circle diameter with respect to the throttle hole is narrower than the opening diameter of the liquid inlet, the projected area of the partition wall is set to 90% or more, and the inner peripheral surface of the inflow chamber following the liquid inlet is defined as the partition wall. It is effective to use a tapered surface that decreases in diameter toward the surface. The area St of the circumscribed circle can be made equal to the projected area of the partition wall.
Also in this case, four collision parts are arranged in a cross shape surrounding the hole center axis in each of the plurality of aperture holes in the processing core part in projection onto a plane orthogonal to the axis of the nozzle body, and the four collision parts The liquid circulation gap can be formed at the center position of the cross formed by the. A set of cross-shaped collision portions formed in the respective restriction holes can be easily formed by four screw members that are screwed so that the tip protrudes into the restriction hole from the wall outer peripheral surface side of the nozzle body. However, if you try to screw as many as four screw members from the outside of the nozzle body into each of a plurality of throttle holes, mistaken geometrical layout may cause interference between the screws, or to a certain throttle hole. There is a problem that the screwed screw member penetrates through another throttle hole. As a result of the study by the present inventors, when the collision portion is formed by the screw portion screwed into the throttle hole from the wall portion outer peripheral surface side of the nozzle body, the most restrictive holes are formed in the partition wall portion without causing such a problem. As a configuration to be formed close to the central region, it is optimal to form a throttle hole in the processing core part by any of two to four in a symmetrical relationship with respect to the central axis of the liquid channel. I found out. In order to avoid the interference of the above-described screw members, it is appropriate that the set of four screw members incorporated in each throttle hole is disposed at a position shifted from each other in the axial direction between the throttle holes. From the viewpoint of suppressing drift and flow loss, the number of throttle holes arranged in this case is preferably 2 to 3, and is optimally 2 in consideration of the ease of nozzle fabrication.
Next, the gas dissolving method of the present invention is characterized in that a mixed phase flow of liquid and gas is supplied to the collision portion of the liquid processing nozzle of the present invention, and the gas is discharged from the liquid outlet in a state of being dissolved in the liquid. To do. The gas dissolving apparatus of the present invention includes the liquid processing nozzle of the present invention, and a multiphase flow supply means for supplying a multiphase flow of liquid and gas to a collision portion of the liquid processing nozzle, and converts the gas into a liquid. It is characterized by being allowed to flow out from the liquid outlet in a dissolved state.
When the liquid is supplied to the liquid processing nozzle of the present invention, a very remarkable strong stirring region is formed around the collision portion and in the immediately downstream region. Bubbles generated by cavitation do not grow so much and are caught in the strong stirring region, and fine bubbles are efficiently generated. However, when gas is actively introduced into the supplied liquid from the outside and supplied to the processing core as a mixed phase flow of liquid and gas, the gas forming the mixed phase flows into the strong stirring region downstream of the collision portion. As a result, mixing with the liquid proceeds remarkably and gas dissolution can be performed very efficiently.
As described above, one of the major factors for creating a strong stirring area in the downstream area of the collision part is the gas dissolved in the liquid to be supplied (Note: The gas introduced from the outside to create a multiphase flow is once dissolved. (Which may also be included) under reduced pressure boiling by cavitation. In the strong stirring region generated in the downstream region of the collision part as a result of the decompression boiling of the dissolved gas, the stirring / dissolution of the gas introduced from the outside proceeds on a scale exceeding the amount of gas impaired by the boiling under reduced pressure. In addition, the gas that could not be dissolved in the liquid remains in the liquid as microbubbles with a very low ascending speed, and various known effects peculiar to microbubbles (for example, cleaning effect, liquid permeability promoting effect, etc.) However, there is also an advantage that is exhibited according to the type of gas. In addition, since the same gas coexists in the liquid in the form of both dissolved gas and fine bubbles, when exposed to an atmosphere that does not have a partial pressure of the same type of gas as the dissolved gas, the liquid that contains only the dissolved gas In comparison, the apparent rate of decrease in dissolved gas concentration decreases and the high concentration state is maintained for a longer time. This is due to the fact that the gas in the fine bubbles elutes into the surrounding liquid, not the evaporation rate of the dissolved gas decreases. As a result, when the liquid is provided for the purpose of requiring a dissolved gas concentration of a certain level or more in an open atmosphere, there is an advantage that the life of maintaining the high concentration can be extended.
In the gas dissolving method of the present invention, as a method of supplying a multiphase flow to the collision part of the liquid processing nozzle, a method of allowing gas to flow upstream from the collision part to the processing core part of the liquid processing nozzle can be adopted. is there. In this method, the flow cross-sectional area is reduced due to the arrangement of the collision part in the processing core part, the flow is restricted, and the gas to be dissolved can be sucked in at a relatively low pressure due to the vacuum suction effect by the venturi effect. Since the gas is supplied at a position close to the part, the introduced gas bubbles are quickly pulverized, and there is an advantage that the dissolution efficiency is easily improved. In this case, as a configuration of the liquid processing nozzle to be used, a gas introduction hole that opens to the outer peripheral surface of the nozzle body and communicates with the throttle hole upstream of at least one of the plurality of collision portions is provided in the nozzle body. The formed one can be used. If a gas supply pipe is connected to the inlet of the gas introduction hole on the outer peripheral surface side of the nozzle, the gas to be dissolved can be easily introduced into the throttle hole. In this case, the multiphase flow supply means of the gas dissolving device of the present invention is configured to include a liquid supply unit that supplies liquid to the liquid inlet of the liquid processing nozzle and a gas supply unit that supplies gas to the gas introduction hole. Just keep it.
On the other hand, in the gas dissolving method of the present invention, a method is adopted in which gas is allowed to flow in the liquid flow path of the liquid processing nozzle upstream of the processing core portion or the liquid supply path upstream of the liquid inlet of the liquid processing nozzle. It may be adopted. In this case, the multiphase flow supply means of the gas dissolving apparatus of the present invention includes a liquid supply unit that supplies liquid to the liquid inlet of the liquid processing nozzle, and a gas that includes a gas supply nozzle independent of the nozzle body connected to the liquid inlet. What is necessary is just to comprise as a thing provided with a supply part.
Since the liquid processing nozzle of the present invention is excellent in gas dissolution efficiency, the simplest method can be used to dissolve the gas while flowing the liquid through the liquid processing nozzle for only one pass. In this case, the multiphase flow supply means (specifically, the liquid supply unit) of the gas dissolving apparatus of the present invention includes a liquid supply pipe connection unit for connecting a liquid supply pipe connected to an external liquid supply source, Liquid discharge for connecting a gas-dissolved liquid discharge pipe to the liquid outlet side so that the gas-dissolved liquid in which gas is dissolved in one pass by the liquid processing nozzle flows out from the liquid outlet of the liquid processing nozzle What is necessary is just to set it as the structure which provided the pipe connection part.
Even with such a simple one-pass dissolution apparatus, the gas can be dissolved at a high concentration by using the liquid treatment nozzle of the present invention. On the other hand, it is also possible to dissolve the gas flowing out from the nozzle while circulating it back to the nozzle via a pump, so that a higher concentration of gas can be dissolved and coexist in the liquid as fine bubbles. The amount of gas can also be increased significantly. In this case, the multiphase flow supply means (specifically, the liquid supply unit) of the gas dissolving apparatus includes a circulation pipe that returns from the liquid storage part that stores the liquid to the liquid storage part via the liquid processing nozzle, and the circulation pipe. A liquid feed pump that circulates and feeds the liquid in the liquid storage part in a form that circulates the liquid processing nozzle while mixing with the gas from the gas supply part and then returns to the liquid storage part can be provided.
In the gas dissolving method of the present invention, the type of the liquid in which the gas is dissolved is not particularly limited. However, as already mentioned, water (including an aqueous solution and a colloidal solution containing water as a solvent) is used. it can. In addition to water, it is an organic liquid such as alcohol (and a diluted product thereof) and fossil fuel (gasoline, light oil, heavy oil, etc.). On the other hand, the type of gas to be dissolved is not limited in the same manner, but may be, for example, oxygen, nitrogen, carbon dioxide, ozone, chlorine, argon, helium, hydrogen, etc., and may be a mixed gas of two or more selected from them. .
Hereinafter, when the liquid is water, the content of the embodiment in which the gas dissolving method of the present invention can exert a remarkable effect will be described. The first case is when carbon dioxide is dissolved. In this case, the mixed phase flow supply means of the gas dissolving apparatus of the present invention is configured to supply a mixed phase flow of carbon dioxide gas and water.
Carbon dioxide has a very high solubility in water, and the saturation solubility at 1 atm (normal pressure: 0.1 MPa) in the case of 20 ° C. water reaches 1800 ppm. For example, in order to obtain high-concentration carbonated water exceeding 500 ppm under normal pressure, carbon dioxide gas exceeding 30% of the volume of water must be dissolved at room temperature, and usually a hollow fiber gas separation membrane is reversely used. Thus, an apparatus for increasing the carbon dioxide dissolution efficiency is used, but the gas dissolution unit using the carbon dioxide separation membrane is very expensive and has a short life. Further, in the gas-liquid mixing method using an ejector or the like, the dissolution efficiency of carbon dioxide gas is low, and it is very difficult to dissolve carbon dioxide gas exceeding 30% of the volume flow rate of water in one pass. However, the liquid processing nozzle of the present invention simply supplies a mixed phase flow of carbon dioxide gas and water to the nozzle. For example, even with a water pressure of about 0.1 MPa or a carbon dioxide gas of about 30% of the volume of water, even one pass Demonstrate the ability to dissolve easily. When the liquid outlet side is opened and water is circulated to the liquid inlet so that the dynamic pressure is 0.1 MPa, the flow rate of water flowing out from the liquid outlet is Q, and this is the total flow cross-sectional area St of the processing core. Standardized water flux Q / St is 0.5L ・ mm ² (Hereinafter, the liquid processing nozzle of the present invention configured in this way is referred to as “standard configuration liquid processing nozzle”). When the carbon dioxide flow rate for forming the multiphase flow is Q1 and the water flow rate is Q2, the dynamic water pressure on the liquid inlet side is 0.015 MPa to 0.3 MPa, and the carbon dioxide / water flow ratio Q1 / Q2 is 0. .1 or more and 1.0 or less (however, if the gas flow rate is a volume flow rate in terms of pressure of 0.1 MPa: the same applies hereinafter), if water and carbon dioxide gas are supplied to the liquid treatment nozzle in one pass or circulatingly, In contrast, it can be dissolved at a dissolution efficiency of 40% or more. It is of course possible to set the dynamic water pressure on the liquid inlet side to a high pressure exceeding 0.3 MPa.
In the case where carbon dioxide gas is dissolved, an aqueous sodium hypochlorite solution can also be used as water. Efficient dissolution of carbon dioxide keeps the pH value of the sodium hypochlorite aqueous solution weakly acidic, for example, around 4.3-6, greatly increasing the concentration of hypochlorous acid in a dissociated state effective for sterilization and disinfection. In addition, the fluctuation of the pH value can be reduced by the pH buffering action peculiar to carbonic acid. For example, compared to the conventional pH adjustment method by adding hydrochloric acid or acetic acid, the phenomenon of undershooting to a low value of 3.5 or less is extremely less likely to occur, thereby suppressing the generation of harmful free chlorine gas. Can do. From the viewpoint of enhancing the effect, it is desirable that the sodium hypochlorite aqueous solution is adjusted to have a hypochlorite ion concentration of 10 ppm to 1000 ppm, and the dissolved concentration of carbon dioxide gas is adjusted to 200 ppm to 1500 ppm. Is desirable. When the hypochlorite ion concentration is less than 10 ppm, the disinfection action is insufficient, and when it exceeds 1000 ppm, the cost of the sodium hypochlorite aqueous solution is increased. In addition, the pH value of the aqueous sodium hypochlorite solution should be stably maintained in the range of 4.3 to 6 where the disinfection effect is optimized by adjusting the dissolution concentration of carbon dioxide gas to 200 ppm to 1500 ppm. Can do.
Further, without using a sodium hypochlorite aqueous solution, carbon dioxide gas may be dissolved in normal water by the method of the present invention, and a sodium hypochlorite aqueous solution may be added later. In this way, the chemical resistance required especially for the material of the collision part of the liquid processing nozzle can be greatly reduced. In this case, the gas dissolving apparatus of the present invention is provided with a sodium hypochlorite aqueous solution supply unit for quantitatively supplying a sodium hypochlorite aqueous solution to the water in which the carbon dioxide gas delivered from the liquid processing nozzle is dissolved. Thus, the above method can be realized.
The second case is when nitrogen is dissolved. In this case, the multiphase flow supply means of the gas dissolving apparatus of the present invention is configured to supply a multiphase flow of nitrogen and water. In the field of water treatment such as boiler water supply, water is deoxygenated in order to prevent corrosion of boilers and piping caused by dissolved oxygen in the water, and one method is nitrogen. The nitrogen-type deoxygenation device removes dissolved oxygen in raw water by bringing the raw water into contact with nitrogen gas, that is, by dissolving the nitrogen gas, in a form replacing nitrogen (referred to as oxygen stripping). . When using the gas dissolution method of the present invention, compared with the conventional method using a venturi tube ejector, a static mixer, etc., the nitrogen gas has a higher melting efficiency, thereby reducing the nitrogen gas flow rate and the circulation time. The oxygen concentration of raw water can be reduced.
When the nitrogen-dissolved water is brought into contact with the atmosphere again, the re-dissolution of oxygen in the atmosphere starts immediately. Therefore, when the conventional method is used to dissolve and deoxygenate nitrogen, the rate of increase in dissolved oxygen concentration is quite fast. . However, when the method of the present invention is used, the introduced nitrogen is contained not only in a dissolved state but also in the form of fine bubbles having a bubble diameter of 1 μm or less, and the dissolution of nitrogen from the bubbles is caused by oxygen from the atmosphere. As a result, the low dissolved oxygen concentration state can be maintained for a long time from several times to several tens of times the conventional one.
When a liquid treatment nozzle having a standard configuration is used, the dynamic water pressure on the liquid inlet side is 0.015 MPa or more and 0.3 MPa or less when the nitrogen flow rate for forming the multiphase flow having the above configuration is Q1 and the water flow rate is Q2. The dissolved oxygen concentration of water can be reduced to 1 ppm or less by supplying the nitrogen / water flow rate ratio Q1 / Q2 to 0.1 or more and 0.3 or less and supplying the liquid treatment nozzle in one pass or circulating supply. In the case of pump circulation, the number of passes for circulating supply means that the pump liquid flow rate is QP (L / min), the circulation time is T (min), and the water volume in the tank is V (L). QP × T / V.
The third case is when oxygen is dissolved. In this case, the multiphase flow supply means of the gas dissolving apparatus of the present invention is configured to supply a multiphase flow of oxygen and water. In fish breeding tanks, ginger for curing live fish (including shellfish), or agricultural water (especially water for hydroponics), fish and plants consume dissolved oxygen in the water, resulting in oxygen constants due to aeration, etc. Replenishment is necessary, and the amount of oxygen consumed in vain due to ascent is large. When the gas dissolution method of the present invention is used, the oxygen gas dissolution efficiency becomes higher compared to the conventional method using a venturi tube ejector, a static mixer, etc., thereby reducing the oxygen gas flow rate and the circulation time. The dissolved oxygen concentration of the raw water can be significantly increased or maintained.
For example, when a liquid processing nozzle having a standard configuration is used, the dynamic water pressure on the liquid inlet side is 0.015 MPa or more and 0.3 MPa when the hydrogen flow rate for forming the multiphase flow having the above-described configuration is Q1 and the water flow rate is Q2. Hereinafter, the hydrogen / water flow ratio Q1 / Q2 is set to 0.1 or more and 0.3 or less, and the dissolved hydrogen concentration of water is set to 0.3 ppm or more and 1.8 ppm or less by supplying the liquid treatment nozzle in one pass or circulation. Can do.
As the gas to be used, pure oxygen may be used, or a mixed gas of nitrogen and oxygen such as air may be used. If oxygen gas with a higher concentration than air is supplied, the dissolved oxygen concentration of the resulting water can be made higher than the atmospheric equilibrium dissolved concentration (about 8 ppm) at room temperature and normal pressure. In the case of using raw water, the level near the equilibrium dissolved oxygen concentration with air can be maintained by dissolving air.
When water in which oxygen is dissolved at a concentration higher than the atmospheric equilibrium dissolved concentration is brought into contact with the atmosphere again, the evaporation of oxygen proceeds until the concentration decreases to the atmospheric equilibrium dissolved concentration. In addition, when fish or shellfish are raised or cured in water, oxygen is consumed by these fish and shellfish, and the oxygen concentration decreases more rapidly. In these cases, when oxygen is dissolved by the conventional method, the rate of decrease in the dissolved oxygen concentration is considerably fast. However, when the method of the present invention is used, the introduced oxygen is contained not only in a dissolved state but also in the form of fine bubbles having a bubble diameter of 1 μm or less, and oxygen depleted by evaporation or consumption is bubbled. As a result of being supplemented by the dissolved oxygen, the high dissolved oxygen concentration state can be maintained for a long time, for example, several times to several tens of times the conventional one. In addition, since the oxygen dissolution efficiency is high, the oxygen supply flow rate required to maintain a high dissolved oxygen concentration state can be greatly reduced even when an oxygen consumer is present.
For example, when a liquid processing nozzle having a standard configuration is used, the dynamic water pressure on the liquid inlet side is 0.015 MPa or more and 0.3 MPa when the oxygen flow rate for forming the multiphase flow having the above configuration is Q1 and the water flow rate is Q2. Hereinafter, the oxygen / water flow ratio Q1 / Q2 is set to 0.1 or more and 0.3 or less, and the dissolved oxygen concentration of water can be set to 10 ppm or more and 40 ppm or less by supplying the liquid treatment nozzle in one pass or circulation.
The fourth case is when hydrogen is dissolved. In this case, the multiphase flow supply means of the gas dissolving apparatus of the present invention is configured to supply a multiphase flow of hydrogen and water. Dissolved hydrogen in water exhibits remarkable reducibility, exhibits an antioxidant effect and an inactivating effect of active oxidative species, and there are many products that are presumed to be taken into the body by drinking or ingestion. Unlike oxygen and nitrogen, hydrogen not only has a low saturation solubility in water, but also has the lowest specific gravity among all gases, so the re-evaporation of dissolved hydrogen is significant, so that high-concentration hydrogen water can be obtained. It has been considered that a pressure dissolution process is essential. However, when the gas dissolution method of the present invention is used, high-concentration hydrogen water can be obtained very simply by passing the liquid treatment nozzle as a mixed phase flow of water and hydrogen without performing pressurization. . In addition, when the method of the present invention is used, the introduced hydrogen is contained not only in a dissolved state but also in the form of fine bubbles having a bubble diameter of 1 μm or less, so that hydrogen depleted by evaporation dissolves from the bubbles. As a result, even in a state open to the atmosphere, compared to hydrogen water containing only dissolved hydrogen by pressurization, the high dissolved hydrogen concentration state is, for example, several times to several tens of times longer than conventional. Will be able to keep. Hydrogen, like nitrogen, has a stripping effect of dissolved oxygen, which can contribute to reducing corrosion of boilers and piping. At this time, dissolved hydrogen exhibits reducibility, and the oxidative corrosion reduction effect is even more remarkable than when nitrogen is used.

The effects of the present invention have already been described in the section of “Means for Solving the Problems” for details of the operation and effects of the present invention, and will not be repeated here.

FIG. 1 is a cross-sectional view and a side view showing a first embodiment of a liquid processing nozzle of the present invention.
FIG. 2 is a side view showing details of a processing core part of the liquid processing nozzle of FIG. 1.
FIG. 3 is an explanatory diagram illustrating the valley arrangement of FIG. 2.
FIG. 4 is an explanatory diagram of the operation of the peaks and valleys in the collision portion.
FIG. 5 is a plan view showing the operation of the collision portion.
FIG. 6 is a side view showing a first modification of FIG.
FIG. 7 is an explanatory diagram showing the valley arrangement of FIG.
FIG. 8 is a side view showing a second modification of FIG.
FIG. 9 is a side view showing a third modification of FIG.
FIG. 10 is a side view showing a fourth modification of FIG.
FIG. 11 is a diagram illustrating a modified example of the formation form of the peaks and valleys.
FIG. 12 is a diagram illustrating an example of a unit in which a plurality of liquid processing nozzles are connected in parallel.
FIG. 13: is a figure which shows the cross section which shows 2nd embodiment of the liquid processing nozzle of this invention with the A arrow expansion.
14 is a cross-sectional view showing details of a processing core portion of the liquid processing nozzle of FIG.
FIG. 15 is an enlarged view of the arrangement in the flow axis direction of the screw member in the processing core portion of FIG. 13.
FIG. 16 is a diagram showing a modified arrangement example of FIG.
FIG. 17 is a diagram showing an embodiment in which a part of a plurality of throttle holes are overlapped and integrated.
FIG. 18 is a view showing a modification in which four screw members of each throttle hole of the liquid processing nozzle of FIG. 13 are arranged on the same plane.
FIG. 19 is a schematic diagram illustrating an example in which three throttle holes are formed in the processing core portion.
FIG. 20 is a view showing a modification in the case where the collision portion and the nozzle body are integrally formed by injection molding.
FIG. 21 is a diagram showing a modification in which four throttle holes are provided and only one screw member that forms a collision portion is disposed in each throttle hole.
FIG. 22 is a view showing a modified example of the arrangement of the screw members in the processing core part.
FIG. 23 is a diagram illustrating an example in which no crest is formed on the entire circumference of the collision portion.
FIG. 24 is a schematic view showing an example in which the liquid processing nozzle of the present invention is incorporated in the middle of a shower hose.
FIG. 25 is a schematic view showing an example in which the liquid treatment nozzle of the present invention is used for toilet flushing of a toilet.
FIG. 26 is a side view showing an example in which a gas introduction hole is provided in the liquid processing nozzle of FIG. 1.
FIG. 27 is a three-view diagram illustrating an example in which a gas introduction hole is provided in the liquid processing nozzle of FIG. 13.
FIG. 28 is a cross-sectional view showing an example of a gas dissolving apparatus that uses the liquid processing nozzle of the present invention to perform dissolution in one pass.
FIG. 29 is a schematic diagram showing an example of how to use the gas dissolving apparatus of FIG.
30 is a cross-sectional view showing an example in which a liquid feed pump is incorporated in the gas dissolving apparatus of FIG.
FIG. 31 is a schematic diagram showing an example of a method of using the gas dissolving apparatus of FIG.
FIG. 32 is a schematic diagram showing an example of an apparatus that uses the liquid processing nozzle of the present invention to perform gas dissolution while pumping liquid.
FIG. 33 is a schematic view showing an example in which the apparatus of FIG. 32 is modified so that ozone can be dissolved.
FIG. 34 is a cross-sectional view showing an example in which a mechanism capable of quantitatively supplying a sodium hypochlorite aqueous solution is added to the gas dissolving apparatus of FIG.
FIG. 35 is a graph showing a weight reduction curve by heating a human hair sample immersed in the treated water of the present invention together with the treated water of the comparative example.
FIG. 36 is a graph showing a weight reduction curve of treated water (Example) of No. 106 in Table 4 together with calculation results of bound water and free water.
FIG. 37 is a graph showing a weight reduction curve of treated water (Example) of No. 107 in Table 4 together with calculation results of bound water and free water.
FIG. 38 is a graph showing a weight reduction curve of treated water of No. 110 in Table 4 (comparative example) together with calculation results of bound water and free water.

DESCRIPTION OF EMBODIMENTS Hereinafter, embodiments for carrying out the present invention will be described with reference to the accompanying drawings.
(Embodiment 1)
FIG. 1 shows a cross section of a liquid processing nozzle and a side surface on the liquid inlet side, showing the first embodiment of the present invention. The liquid processing nozzle 1 includes a nozzle body 2 in which a liquid channel 3 is formed. The nozzle body 2 is formed in a cylindrical shape, and a liquid passage having a circular cross section is formed in the direction of the central axis O thereof. The liquid channel 3 has a liquid inlet 4 at one end (right side in the drawing) and a liquid outlet 5 at the other end, and has a diameter smaller than that of the liquid inlet 4 and the liquid outlet 5 at an intermediate position in the flow direction. A throttle hole 9 is formed. The liquid flow path 3 has an inflow chamber 6 on the liquid inlet 4 side than the throttle hole 9 and an outflow chamber 7 on the liquid outlet 5 side, and a collision portion 10 is provided in a protruding form from the inner surface of the throttle hole 9. The core part CORE is formed.
FIG. 2 is an enlarged view when the throttle hole 9 is viewed from the side, and the collision part 10 is formed so that a plurality of crests 11 in the circumferential direction and troughs 12 as high flow velocity parts are alternately connected to the outer peripheral surface. Yes. In this embodiment, the collision part 10 is a screw member (hereinafter, also referred to as “screw member 10”) whose leg end side protrudes into the flow path, and as a result, a plurality of ridges 11 formed in the collision part. Are integrally formed in a spiral shape.
The material of the nozzle body 2 is, for example, a resin such as ABS, nylon, polycarbonate, polyacetal, or PTFE, but may be a metal such as stainless steel or brass, or a ceramic such as alumina, and is appropriately selected depending on the application. The material of the screw member 10 is, for example, stainless steel. However, depending on the application, a heat-resistant alloy such as titanium, hastelloy, or Inconel (both are trade names) having higher corrosion resistance may be used. In case of a problem, it is possible to use a ceramic material such as quartz or alumina. In particular, it is preferable to use quartz for application to a field that dislikes metal contamination (for example, the semiconductor field), and the nozzle body 2 made of resin is preferably made of PTFE, for example.
In the processing core part CORE in FIG. 1, the set of collision parts formed in the throttle hole 9 protrudes into the throttle hole 9 from the outer peripheral surface side of the wall part with respect to the screw hole 19 formed in the nozzle body 2. It is formed by four screw members screwed in. The setting between the screw hole 19 and the screw member 10 is fixed by an adhesive or the like. As shown in FIG. 2, a main flow region 21 is formed between the screw member (impact portion) 10 and the inner peripheral surface of the throttle hole 9. In each throttle hole 9, a liquid flow gap 15 is formed at the center position of the cross formed by the four collision portions 10. The front end surfaces of the four collision portions 10 forming the liquid flow gap 15 are formed flat, and the liquid flow gap 15 is formed in a square shape in the above-described projection.
Next, in FIG. 2, the total area inside the outer peripheral edge of the projection region of the liquid flow path in the processing core part, here, the area of the circular axis cross section of the throttle hole 9 in FIG. 4) is S1, and the projected area of the collision part 10 (four screw members) is S2, and the total flow cross-sectional area St of the processing core part is
St = S1-S2 (unit: mm ² )
Define as In this embodiment, the total area of the main flow area 21 and the liquid flow gap 15 corresponds to the total flow cross section St. As shown in FIG. 1, the opening diameters of the liquid inlet 4 and the liquid outlet 5 are larger than the inner diameter of the throttle hole 9. That is, the cross-sectional areas of the liquid inlet 4 and the liquid outlet 5 are set larger than the total flow cross-sectional area St. Further, the inner peripheral surfaces of the inflow chamber 6 and the outflow chamber 7 connected to the throttle hole 9 are tapered portions 13 and 14, respectively.
FIG. 3 is the same projection view as FIG. 2, and the reference numerals are omitted (therefore, the reference numerals of the respective parts are the same as those in FIG. 2). The depth h of the valley portion 21 that appears in the projected outline of the screw member (impact portion) 10 is secured to 0.2 mm or more. Further, a circle drawn with a radius corresponding to 70% of the distance from the projection point of the central axis O to the inner peripheral edge of the liquid channel is a reference circle C. ₇₀ Among the valley points representing the bottom position of the valley portion 21, the reference circle C ₇₀ N is the number of items located inside (hereinafter referred to as 70% valley score: indicated by ○) ₇₀ (Pieces), standard circle C ₇₀ Nc is the number of those located outside (hereinafter referred to as 70% complement valley points: indicated by ●) ₇₀ (Pieces).
Then, the valley depth correction coefficient α is determined according to the above-described equation (1) according to the thread valley depth h to be employed. Further, in the projection shown in FIG. ₇₀ The area of the part located inside ₇₀ (Unit: mm ² ) 70% section ratio σ ₇₀ The
σ ₇₀ = S ₇₀ / St x 100 (%)
Determine as Assuming the above, the liquid processing nozzle 1 of FIG. 1 has an effective valley point number Ne defined by the above-described equation (2), and an effective valley point density (Ne / St) normalized by the total flow cross-sectional area St. 1.5 / mm ² Or more (preferably 1.8 pieces / mm ² This is ensured. Specific examples of values of effective valley point density when the inner diameter D of the throttle portion, the outer diameter M of the screw member 10 and the valley depth h are variously set are as shown in Tables 1 to 6 described later.
For example, the operation when water is circulated to the liquid processing nozzle 1 of FIG. 1 so that the dynamic pressure is about 0.1 MPa through the liquid inlet 4 by opening the liquid outlet 5 side will be described. This water is, for example, tap water, and it is assumed that air is dissolved at a concentration that is in equilibrium with the atmosphere (for example, the oxygen concentration at 20 ° C. (normal temperature) is about 8 ppm). The water flow is first squeezed by the taper portion 13 and the throttle hole 9, and then into a liquid circulation region composed of the main circulation region 21 and the liquid circulation gap 15 of FIG. 2 formed between the screw member 10 and the inner peripheral surface of the throttle hole 9. And passes through the screw member 10 while colliding with it.
When passing through the outer peripheral surface of the screw member 10, as shown in FIG. 4, the flow forms a high speed region in the valley portion 12 and a low speed region in the peak portion 11. Then, the high-speed region of the valley portion 12 becomes a negative pressure region by Bernoulli's theorem, and bubbles FB are generated by cavitation, that is, decompression precipitation of dissolved air. A plurality of valleys are formed on the outer periphery of the screw member 10, and four screw members 10 are arranged in the throttle hole 9, so this reduced pressure deposition occurs simultaneously and frequently in the valleys in the throttle hole 9. Will happen. Then, as shown in FIG. 5, when the water flow collides with the screw member 10, the reduced pressure precipitation in the valley portion occurs violently, and this is further entangled in the vortex generated when detouring downstream of the screw member 10. Stir vigorously. Thereby, the remarkable strong stirring area | region SM containing the countless micro eddy current FE is formed in the circumference | surroundings and the immediate downstream area of the collision part 10. FIG. The reduced pressure region where the bubbles are deposited is limited to the vicinity of the valley bottom around the collision part 10, and the high-speed liquid flow passes through the region almost instantaneously. Fine bubbles with a bubble diameter of less than 1 μm are efficiently generated by being caught in the stirring region.
The cavitation efficiency, and therefore the fine bubble generation efficiency, dominates the valley density obtained by normalizing the absolute number of valleys with the channel cross-sectional area, but the flow velocity in the pipe is maximum near the center of the pipe axis cross section. The parabolic distribution is shown in the radial direction in a shape that becomes the minimum at the inner wall surface position. For example, it is ideal to calculate the flow velocity distribution in the entire cross section by computer simulation using the finite element method, etc., and to determine the weighting factor according to the flow velocity for each valley point position, but it takes a very long time for the simulation. Cost. Therefore, in the present invention, as a simple method, the reference circle C is positioned at a position where the flow velocity is approximately 50% of the maximum value at the center of the cross section in the cross section without the collision portion. ₇₀ And the number of valleys inside the reference circle (70% valley points) N ₇₀ On the other hand, the number of valleys on the outer side (70% complement valley number Nc ₇₀ ) Is weighted 0.38 times and added.
In addition, in order for valley points located near the center of the cross section to effectively contribute to the cavitation effect, it is necessary to obtain the expected flow velocity near the center of the cross section. The score needs to be evaluated by giving a weight to the distribution area near the center of the cross section. 70% section ratio σ ₇₀ If there is no collision part, the value is 50%. Therefore, even when the collision part is arranged, the valley point inside the reference circle has a higher flow velocity as the 70% cross-sectional ratio value approaches 50%. 70% valley score N ₇₀ Is σ ₇₀ Weighted by a value of / 50. Then, the influence of the valley depth h is weighted by the valley depth correction coefficient α in the above-described equation (1) regardless of the inside / outside of the reference circle, and the above-mentioned (3) as the effective valley point number Ne. It can be calculated as an equation. The effective valley point density Ne / St obtained by normalizing the effective valley point number Ne with the total flow cross-sectional area St of the processing core portion is an index for objectively quantifying the fine bubble generation capability of the liquid processing nozzle. 1.5 / mm ² Or more (preferably 1.8 pieces / mm ² When the above is ensured, the cavitation efficiency and thus the generation efficiency of fine bubbles are remarkably improved.
As shown in FIG. 6, the collision portion may be formed by two screw members 10 screwed in the diameter direction. In this configuration, the liquid flow gap 15 is formed between the tip surfaces of the two screw members 10 and 10. In this configuration, as shown in FIG. 7, the reference circle C is equivalent to the amount that the tip of the screw member 10 approaches the center of the cross section of the throttle hole 9. ₇₀ It can be seen that a valley point can be arranged at a position closer to the center on the inside. However, when the cross-sectional diameter of the throttle portion 9 increases, the effective valley point density Ne tends to be low, so that it can be said that the total flow cross-sectional area St is relatively small and suitable for a small flow rate liquid processing nozzle. FIG. 8 shows an example in which the collision portion is constituted by one screw member 110 in the diameter direction.
As shown in FIGS. 9 and 10, a plurality of crests 111 and troughs 112 (which can be formed by rolling, for example) that are not spirally integrated are closed in the axial direction of the collision parts 120 and 130. You may arrange. In FIG. 9, the crest 111 is formed in parallel with the plane orthogonal to the axis of the collision part 120, and in FIG. 10, the crest 111 is formed in parallel with the plane intersecting with the axis of the collision part 120. .
In addition, as shown in FIG. 12, a nozzle unit 600 is formed by connecting a plurality of liquid processing nozzles 1 of FIG. In this way, even when the inner diameter of the throttle hole of the nozzle 601 is set small so as to prioritize securing the flow velocity, the flow rate per nozzle is small, but the entire unit 600 is sufficient without sacrificing the cavitation effect. The flow rate can be secured. In this embodiment, both ends of the liquid processing nozzle 1 are formed in a straight shape, and the branch joint 602 is configured such that the branch side connection portion connects the ends of the nozzle with one touch, and the connection portion on the flow unification side is a normal screw joint. It is configured as.
The crests and troughs do not necessarily have to be formed all around in the circumferential direction of the collision part, as shown in FIG. 23, on the downstream side in the flow direction (white arrow) that does not easily function as a cavitation point. The crest 12 and the trough 10 may be cut out in a partial section in the circumferential direction by forming an axial groove 10a or the like on the outer peripheral surface of the collision unit 10. FIG. 11 is a three-dimensional conceptual diagram showing an example of the collision part 140 in which the mountain parts 141 are intermittently formed in the circumferential direction. Although the peak portion 141 is formed as a series of pyramidal protrusions in FIG. 11, there is no change in that a valley portion 142 is formed at the projection side edge of the collision portion 140.
Note that the tip of the screw member (impact portion) is not limited to that shown in FIG. 2, and other various forms can be adopted. For example, the tip of the screw member 10 may be formed in a conical shape, and in this case, the liquid flow gap is formed in a cross shape.
(Embodiment 2)
FIG. 13: shows the cross section of the liquid processing nozzle which shows the 2nd of embodiment of this invention with the enlarged side surface from the axial direction (A arrow) on the liquid inlet side. The liquid processing nozzle 151 includes a nozzle body 2 in which a liquid channel 3 is formed. The nozzle body 2 is formed in a cylindrical shape, and a liquid passage having a circular cross section is formed in the direction of the central axis O thereof. The nozzle body 2 includes a partition wall 8 that divides the liquid flow path 3 into an inflow chamber 6 on the liquid inlet 4 side and an outflow chamber 7 on the liquid outlet 5 side, and an inflow chamber 6 and an outflow chamber formed through the partition wall 8. A processing core portion CORE is formed that includes a plurality of throttle holes 9 that communicate with each other through different paths and a collision portion 10 that protrudes from the inner surface of the throttle hole 9. In FIG. 13, two throttle holes 9 are formed in the partition wall portion 8 with the same inner diameter so as to be an axial object with respect to the central axis O. In the projection on the plane orthogonal to the axis O of the nozzle body 2 in the same form as in FIG. 2 (and FIG. 3), the impinging portion 10 is formed in each of the plurality of restricting holes 9 in the processing core portion CORE. Four are arranged in a cross shape surrounding the central axis 9. In each throttle hole 9, the effective valley point density Ne defined by the above equation (1) is 1.5 / mm. ² Or more (preferably 1.8 pieces / mm ² This is ensured.
Each set of collision portions formed in the throttle hole 9 is formed by four screw members that are screwed so that the tip protrudes into the throttle hole 9 from the wall outer peripheral surface side of the nozzle body 2. As indicated by a broken line in the enlarged view of arrow A, the screw member 10 is screwed into a screw hole 19 formed through the wall portion of the nozzle body 2, and the screw head lower surface is located in the middle of the screw thrust direction of each screw hole 19. A stepped surface 19r is formed to support the. The formation position of the stepped surface 19r is such that when the screw member 10 is screwed in, the length of the screw leg portion protruding into the throttle hole 9 (that is, the portion serving as the collision portion) forms the liquid flow gap 15. It has been adjusted to be appropriate. The setting between the screw hole 19 and the screw member 10 is fixed by an adhesive or the like.
In addition, since the screw hole 19 opens in the outer peripheral surface of the nozzle main body 2, the cylindrical cover 18 which covers the outer peripheral surface of the nozzle main body 2 is attached by adhesion etc. in order to conceal this. The outer peripheral surface of the cover member 18 may be decorated by plating or painting. In addition, an inflow side connection portion 16 and an outflow side connection portion 17 are formed on the outer peripheral surfaces of both ends of the nozzle body 2.
Further, as shown in FIG. 14, in order to avoid interference of the screw members 10 between the plurality of throttle holes 9, a set of four screw members 10 incorporated in each throttle hole 9 is arranged between the throttle holes 9. They are arranged at positions shifted from each other in the axial direction. Further, in FIG. 14, the plurality of screw members 10 </ b> A, 10 </ b> B, 10 </ b> C, 10 </ b> D in the same throttle hole 9 are arranged at positions shifted from each other in the axial direction (flow direction) of the throttle hole 9. . Specifically, in each throttle hole 9, screw member pairs 10A, 10B and 10C, 10D arranged at positions orthogonal to each other on the same plane are different from each other in the flow direction (in FIG. The holes 9 are arranged at positions A and B on the downstream side, and the positions of the lower throttle holes are arranged at positions C and D on the upstream side. In the projection onto the plane orthogonal to the central axis O in FIG. 13, the four screw members 10A and 10B at the positions A and B and the four screw members 10C and 10D at the positions C and D respectively form a cross shape. Will be arranged as follows.
In FIG. 14, each pair of screw members 10 is in contact with the outer peripheral edge of the front end surface (or in a form in which the outer peripheral edge of the front end surface is brought closer through a gap narrower than the liquid flow gap). A square liquid flow gap is formed together with the screw member 10 shown in FIG. 22, and FIG. 22 shows a modification of the arrangement of each screw member pair. In FIG. 22, in each of the two pairs 10A, 10B of screw members, the leg end 10b of one screw member is positioned at the center of the throttle hole 9, while the other screw is provided on the peripheral side surface of the leg end 10b. The tip end face 10e of the member is brought into contact (or opposed through a gap), and the leg end 10b on the side located in the center of the throttle hole 9 is placed between the pair in the axial direction of the nozzle body 2 (FIG. 13). They are shifted from each other. In this way, the valley portion of the leg end 10b can be arranged near the center of the throttle hole 9 having a high flow velocity, and the cavitation effect and, consequently, the bubble refining effect can be further enhanced.
Returning to FIG. 13, when four screw members 10 are to be screwed into the respective throttle holes 9 from the outside of the nozzle body 2, if the geometric layout is wrong, interference between the screws, Problems such as a screw member 10 screwed into a certain throttle hole 9 penetrating through another throttle hole 9 are likely to occur. In FIG. 13, the number of throttle holes 9 is two. However, when the impact member is formed by screwing the screw member 10 from the wall outer peripheral surface side of the nozzle body 2 toward the throttle hole 9, It is optimal to form any one of 2 to 4 in a symmetric positional relationship with respect to the 3 central axis.
Next, in FIG. 13, the aperture 9 is defined as L / de, where de is the diameter of a circle equivalent to the sum of the axial cross-sectional areas of the apertures 9 and L is the length of the aperture 9. The hole aspect ratio is set to 3.5 or less. In FIG. 15, in the general case where the inner diameters of the two throttle holes 9 are different from each other (d1, d2), the throttle hole aspect ratio is L / (d12 + d22) 1/2. In FIG. 13, the two throttle holes 9 are formed to have a cylindrical surface having the same inner diameter and the same length, and the inner diameter of the two throttle holes 9 is d, and the throttle hole aspect ratio is 0.71 L / d. It is. The value of the aperture hole aspect ratio L / de is desirably 3 or less, and more desirably 2.5 or less.
In FIG. 13, in the projection onto the plane orthogonal to the axis O of the nozzle body 2, the distance from the reference point O determined at the center position of the projection area of the partition wall 8 to the inner periphery of the plurality of aperture holes 9 (the aperture holes). The plurality of throttle holes 9 are arranged around the reference point O so that the displacement (T) is smaller than the inner diameter D of the throttle hole 9. The throttle hole displacement T is desirably ½ or less of the inner diameter D of the throttle hole 9. Furthermore, in the present embodiment, when the area of the circumscribed circle 20 with respect to the inner periphery of the plurality of apertures 9 is St and the total area of the projection area of the apertures 9 is Sr in the same projection, K≡Sr / St The defined aperture hole aggregation rate K is 0.2 or more.
That is, the liquid processing nozzle 151 satisfies the following conditions.
A throttle hole aspect ratio defined by L / de is 3.5 or less;
The throttle hole displacement T is smaller than the inner diameter D of the throttle hole 9;
-The throttle hole aggregation rate K is 0.2 or more.
Further, the area St of the circumscribed circle 20 is 90% or more (100% in FIG. 13) of the projected area of the partition wall 8. Since the area of the flow blocking region formed outside the throttle hole 9 in the partition wall 8 is small, the flow stagnation and the loss due to the vortex that are generated in such a region are reduced. As is clear from FIG. 13, the diameter of the circumscribed circle 20 with respect to the throttle hole 9 is narrower than the opening diameter of the liquid inlet 4, and the inner peripheral surface of the inflow chamber 6 following the liquid inlet 4 faces the partition wall portion 8. The tapered surface 13 is reduced in diameter.
Further, as shown in FIG. 15, the length of the section located downstream of the collision portion 10 of the throttle hole 9 (hereinafter referred to as the remaining section) is Lp (average value of Lp2 to Lp4), and the axial break of the throttle hole 9 is performed. The remaining section aspect ratio defined by Lp / de is set to 1.0 or less, where de is the diameter of the circle equivalent to the total area. The inner peripheral surface of the outflow chamber 7 is also a tapered surface 14 that expands toward the liquid outlet 5. In FIG. 15, the length of the remaining section is zero for the screw member 10A located on the most downstream side, but as shown in FIG. 16, when the remaining section has a non-zero length Lp1 for the screw member 10A, The remaining section length Lp is an average value of Lp1 to Lp4.
In the liquid processing nozzle 151 of FIG. 13, a plurality of constricted portions are formed in the partition wall portion 8, and the flow path sections before and after the constriction portion are aggregated into the inflow chamber 6 or the outflow chamber 7 defined by the partition wall portion 8. By adopting a structure that is shared by a plurality of throttle portions, the section where the flow path branches into a plurality of systems is only the throttle holes 9 formed in the partition wall portion 8.
According to this configuration, the throttle hole aspect ratio defined by L / de (see FIG. 15) is set to 3.5 or less, and the length of the branch section that causes the drift, that is, the collision portion 10 Can be sufficiently shortened. In addition, the throttle holes 9 are arranged close to the reference point O to such an extent that the throttle hole displacement T (see FIG. 13) is smaller than the inner diameter D of the throttle hole 9, and the partition wall portion 8 having a high flow velocity. Is centralized in the center. As a result, a decrease in flow velocity or non-uniformity in the throttle hole 9 is suppressed, and drift can be reliably prevented. That is, it is possible to achieve both a sufficient cavitation effect and a sufficient flow rate by forming a plurality of throttle holes 9 having the collision portion 10, and the drift between the plurality of throttle holes 9 is effectively suppressed, The generation of fine bubbles based on the cavitation effect can be continued stably.
Further, in the liquid processing nozzle 151 of FIG. 13, the remaining section aspect ratio (see FIG. 15) defined by Lp / de is set to 1.0 or less. By the time the liquid that has passed through the impingement part 10 in the throttle hole 9 merges in the outflow chamber 7, the passage distance of the remaining section of the throttle hole 9 with a large fluid resistance of the flow including the precipitated bubbles is shortened. Since the strong stirring region generated downstream of the collision part 10 of each throttle hole 9 is integrated in the outflow chamber 7, the effect of refining the bubbles is further enhanced.
Hereinafter, modifications of the liquid processing nozzle of FIG. 13 will be listed. Since there are many common points with the liquid processing nozzle of FIG. 13, the same reference numerals are given to common components, and the differences will be mainly described. First, as shown in FIG. 17, the plurality of throttle holes 9 may be integrally formed so as to partially overlap in a region including the center of the partition wall portion 8 in the above-described projection. It is desirable that the projected area of the overlap region be within 30% of the area of each aperture 9.
In the liquid processing nozzle 51 shown in FIG. 18, a set of four screw members 10 arranged in each throttle hole 9 is arranged on the same plane as shown in the sections AA and BB. FIG. 19 shows an example in which three throttle holes 9 are formed in the partition wall portion 8. The positions of the screw members 10 in the flow direction between the three throttle holes 9 are determined to be shifted from each other. Further, in the above-mentioned projection, the three aperture holes 9 are arranged at positions that form the vertices of the equilateral triangle with a distance larger than the inner diameter of the screw hole 9, and the four screw members 10 having a cross-like arrangement are arranged. The arrangement angle of the set of the screw members 10 is determined so that the screw holes 19 extending toward the pair of the remaining throttle holes 9 pass through the pair of the throttle holes 9 in one throttle hole 9. Yes. Accordingly, all the screw holes 19 can be formed so as to open to the outer peripheral surface of the nozzle body 2 without interfering with the throttle hole 9.
FIG. 20 shows an example in which the collision part 10F is formed integrally with the partition part 8 of the nozzle body 2 by injection molding. Naturally, since the material of the collision part 10F is a resin (for example, ABS or nylon) that can be injection-molded, it is necessary to limit the flux within a range where wear due to cavitation is not a problem. In order to integrally mold the collision portions 10F of the plurality of throttle holes 9, the first mold core for forming the inflow chamber so that the central axes of all the collision portions 10F are located on the same plane And a mold cavity of the collision portion 10F and the partition wall portion 8 is provided on each tip surface of the second mold core for forming the outflow chamber, and the mold core is molded in a state where the mold cores are abutted with each other using the plane as a dividing surface. You can do that.
FIG. 21 shows an example in which four throttle holes 9 are formed in the partition wall portion 8. Each of the four throttle holes 9 has a collision portion formed by screwing one screw member 10 in the diameter direction. Specifically, the four throttle holes 9 are arranged at positions that form the vertices of squares in the above-described projection, and the central axis O of the nozzle body 2 from the outer peripheral surface side of the nozzle body 2 to each throttle hole 9. The screw member 9 is screwed in the diameter direction of the throttle hole 9 toward. The screw member 10 may be incorporated into the nozzle body 2 by insert molding, and the collision portion may be integrated with the nozzle body 2 by injection molding, as in FIG.
(Embodiment 3)
Hereinafter, usage examples of the liquid processing nozzle of the present invention (that is, embodiments of the liquid processing method) will be described. 24 may be the liquid processing nozzle 1 of FIG. 1 (the liquid processing nozzle 151 of FIG. 13 or the liquid processing nozzle 51 of FIG. 18) in the middle of a shower hose flow path for a general bathroom (or for a business such as a beauty salon). : The following is the same), and the treated hot water (that is, hot water containing fine bubbles) can be ejected from the shower head. A first hose connection for connecting the liquid treatment nozzle 1 to the nozzle main body 2 of FIG. 1 via the inflow side hose 405 as the inflow side connection portion 16 on the liquid inlet 4 side and the hot water / water mixing tap 408 of FIG. A second hose connection screw for connecting the shower head 401 and the liquid processing nozzle 1 by the outflow side hose 402 as the outflow side connection portion 17 on the liquid outlet 5 side is a thread portion (hereinafter referred to as reference numeral 16). Each part (hereinafter referred to as reference numeral 17) is formed. Each screw portion 16 and 17 is formed as a male screw portion (for example, R1 / 2 to G1 / 2), and the hoses 402 and 405 are connected to the shower head 401, the faucet fittings 403, 404, 406, and 407, respectively. The liquid processing nozzle 1 and the hot / cold water mixing tap 408 are connected. If the hot and cold mixing tap 408 is opened in this state, hot water is supplied to the liquid nozzle 1 and sprayed from the shower head 401. Even when using an existing shower head that does not have the function of generating bubbles, a large amount of fine bubbles can be mixed into the hot water when passing through the liquid processing nozzle 1, increasing the water permeability to the human skin and hair and keeping the moisture. You can enjoy the effects of improving the skin, effectively removing dirt on the scalp and body surface. And even if the nozzle 1 is connected to the middle of the shower hose, it is difficult to be affected by the drift, and the effect of generating fine bubbles can be stably enjoyed.
FIG. 25 shows an example in which the liquid processing nozzle 1 is used for toilet cleaning. A flush water supply pipe 103 is connected to the toilet bowl 105 of the toilet, and washing is performed by supplying and flowing flush water 109 along the inner surface of the toilet bowl via the pipe 103. The liquid treatment nozzle 1 of the present invention is provided in the middle of the washing water supply pipe 103, and the washing water in the pipe is supplied to the toilet 105 after becoming the fine bubble-containing water 109 when passing through the liquid treatment nozzle 1. The toilet 105 and the sewage drain pipes 107 and 108 of the toilet 105 are washed. Thereby, the toilet bowl 105 and the sewage drain pipes 107 and 108 can be kept clean for a long period of time, and adhesion and accumulation of urinary stones and the like are less likely to occur.
In the example of FIG. 25, the toilet 105 is configured as a urinal, and a well-known valve unit 104 with a sensor is provided at a position where the user of the toilet 105 can be detected on the way of the washing water supply pipe 103. Clean water from the water pipe 102 is stored in a wash water tank 101 provided above, and a supply pipe 103 is connected to the wash water tank 101. The sensor-equipped valve unit 104 transitions from the standby state to the cleaning preparation state when the detection state of the user approaching the toilet 105 is continued for a predetermined time or more. In the cleaning preparation state, as the user moves away from the toilet bowl 105 and enters a non-detection state, the valve is opened and a necessary amount of washing water is allowed to flow into the toilet bowl 105, and then the valve is closed again to wait for washing. Return to. The wastewater from the toilet is collected in the sewage pipe 108 and discharged to the sewer or septic tank. The drainage after washing passes through an individual drainage pipe 107 communicating with the lower side of the toilet 105, is collected in a sewage pipe 108 together with drainage from other toilets (not shown), and is discharged toward a sewer or septic tank.
(Embodiment 4)
Next, a specific embodiment of the gas dissolving method using the liquid processing nozzle of the present invention will be described. FIG. 26 shows an example of a liquid processing nozzle in which the liquid processing nozzle 1 and the processing core unit CORE of FIG. The liquid processing nozzle 171 is opened to the nozzle body 2 on the outer peripheral surface of the nozzle body 2 and, as shown in FIG. 1, introduces gas that communicates with the throttle holes 9 upstream of the plurality of collision portions 10. A hole 28 is formed.
When liquid is supplied to the liquid supply port 3 of the liquid processing nozzle 171, a very remarkable strong stirring region SM is formed in the periphery and the immediately downstream region of the collision unit 10 as in FIG. 5. In this state, when a gas to be dissolved is introduced into the gas introduction hole 28 of FIG. 1 and supplied to the processing core unit CORE as a mixed phase flow of liquid and gas, the gas forming the mixed phase flow is strongly downstream of the collision unit 10. By being involved in the stirring region SM (FIG. 5), mixing with the liquid proceeds remarkably, and gas dissolution can be performed very efficiently. The factor that forms the strong stirring region SM in the downstream region of the collision unit 10 is reduced-pressure boiling precipitation caused by cavitation of gas originally dissolved in the liquid supplied from the liquid inlet 4. A strong stirring region SM is formed in the downstream region of the collision unit 10 due to the decompression boiling of the dissolved gas, and an infinite number of fine vortex flows FE are formed, and the gas introduced from the gas introduction hole 28 is entrained therein. The stirring and dissolution of gas proceeds on a scale that is orders of magnitude greater than the amount of gas damaged by boiling under reduced pressure. And the gas that could not be dissolved in the liquid also stays in the liquid as microbubbles with very low ascending speed, and various known effects peculiar to microbubbles (for example, cleaning effect, liquid permeability promoting effect, etc.) Will be exhibited according to the type of gas. In addition, since the same gas coexists in the liquid in the form of both dissolved gas and fine bubbles, when exposed to an atmosphere that does not contain dissolved gas, compared to a liquid in which only dissolved gas exists, apparent dissolved The rate of decrease in gas concentration decreases, and a high concentration state is maintained for a longer time.
In addition, the structure which does not provide a gas introduction hole in the nozzle main body 2 like the liquid processing nozzle 1 of FIG. 1 is adopted, and gas flows in on the liquid supply path upstream from the liquid inlet 4 to form a multiphase flow. It is good also as a system.
Next, the liquid processing nozzle 71 of FIG. 27 has the same configuration as that of FIG. 13, and the screw members 10 arranged at positions orthogonal to each other on the same plane in each throttle hole 9 as shown in FIG. 14. Are arranged at different positions in the flow direction (in the drawing, the positions of A and B on the downstream side for the upper throttle hole 9 and the positions C and D on the upstream side for the lower throttle hole). Yes. In FIG. 27, the gas introduction hole 28 is the most downstream screw member with respect to the nozzle hole 9 on the upper side of the drawing in which the screw member 10 is attached to the position A or B on the downstream side of the two throttle holes 9. A hole is formed in the radial direction with respect to the wall portion of the nozzle body 2 so as to open upstream from the 10A position. A female screw hole 29 for attaching a gas introduction joint 30 for connecting a gas supply pipe is formed in the opening of the gas introduction hole 28 on the outer peripheral surface side of the nozzle body 2. In FIG. 27, the gas introduction hole 28 is opened upstream of any of the screw member pairs 10A and 10B. However, the arrangement interval in the flow direction of the screw member pairs 10A and 10B is widened, so that the gas introduction hole 28 is at an intermediate position between them. The gas introduction hole 28 may be opened.
26 and 27, the gas to be dissolved in the throttle hole 9 can be easily introduced by connecting the gas supply pipe to the gas introduction joint 30 (gas supply unit). In the configuration of FIG. 27, both end portions of the nozzle body 2 of the liquid processing nozzle 71 are a straight inflow side connection portion 26 and an outflow side connection portion 27 for connecting a one-touch fitting (not shown). An intermediate portion in the axial direction connecting the gas introduction joint 30 is a bowl-shaped portion 2 a having a larger diameter than the inflow side connection portion 26 and the outflow side connection portion 27.
Also in the liquid processing nozzle 71, the throttle hole aspect ratio of the throttle hole 9 formed in the partition wall portion 8 is set to 3.5 or less, and the throttle hole displacement is set to the inner diameter D of the throttle hole 9, just like the nozzle 151 in FIG. It is arranged close to the center of the partition wall 8 (around the reference point) so as to be smaller. Further, the length Lp of the remaining section located downstream from the collision portion 10 of the throttle hole 9 is set so that the aforementioned remaining section aspect ratio is 1.0 or less. In this embodiment, since the gas introduction hole 28 is formed only in one of the two throttle holes 9, the gas phase to be dissolved is supplied to the one throttle hole 9 in a biased manner.
However, since the throttle hole aspect ratio is set to 3.5 or less, the flow loss in the entire processing core part CORE is small, and gas is also introduced into the flow F2 in the throttle hole 9 on the gas introduction side. As a result, the flow rate is lower than the flow F1 in the other throttle hole 9, but this is not excessively impaired. And since the remaining section length Lp is small, the introduced gas can be promptly guided to the strong stirring region combined and enlarged downstream of the collision portion 10. That is, the flow from the throttle hole 9 on the gas introduction side can be shared by the outflow chamber 7 in the strong stirring region SM mainly formed on the throttle hole 9 side where the gas is not introduced. Despite the fact that the gas flows in a biased manner in one of the throttle holes 9, extremely efficient gas dissolution and pulverization is possible.
Of course, the gas introduction holes 28 may be provided for all the throttle holes 9, and in this case, the gas is supplied while being distributed to the respective throttle holes 9 (impact portions 10 thereof). Also here, as shown in FIG. 13, a configuration in which a gas introduction hole is not provided in the nozzle body 2 is adopted, and a gas is caused to flow in a liquid supply path upstream from the liquid inlet 4 to form a multiphase flow. Also good. In this method, since the reduced pressure suction effect at the throttle portion cannot be used when supplying the gas, it is necessary to slightly increase the gas supply pressure, but there is an advantage that the gas can be supplied uniformly to each throttle hole 9 of the liquid processing nozzle 1. is there. Further, a configuration in which a gas introduction hole is provided in the inflow chamber 6 upstream of the throttle hole 9 is also possible.
In the gas dissolving method of the present invention, the simplest method is to dissolve the gas while flowing the liquid through the liquid processing nozzle for only one pass. FIG. 28 shows an example of the gas dissolving apparatus of the present invention that can embody the method, and FIG. 29 shows an example of its use. In the gas dissolving apparatus 200, a liquid supply pipe (inflow hose) 405 (a liquid supply unit that forms a mixed phase flow supply means) is connected to an external liquid supply source (for example, a hot-water mixing tap 408 of a water supply or a water heater) (FIG. 27). 27), a liquid supply pipe connecting portion 202B (having a mounting screw portion 202r) is connected. A liquid processing nozzle 71 shown in FIG. 20 is provided at the tip of the liquid supply pipe connecting portion 202B, and gas is supplied from the liquid outlet to the liquid processing nozzle 71 (or the liquid processing nozzle 171 shown with the aid of FIG. 1). The gas-dissolved liquid in which the gas is dissolved in one pass flows out. On the liquid outlet 5 side, a liquid discharge pipe connecting portion 202A (having a mounting screw portion 202r) for connecting a gas-dissolved liquid discharge pipe (outflow side hose) 408 (FIG. 29) is provided. Although the gas dissolving apparatus 200 is a simple one-pass, the gas can be dissolved at a high concentration by using the liquid processing nozzle of the present invention.
Hereinafter, the details of the gas dissolving apparatus 200 will be further described. The gas dissolving apparatus 200 includes a main body case 201, and a liquid discharge pipe connecting portion 202A and a liquid supply pipe connecting portion 202B each made of a metal threaded pipe joint are attached to the surface of the main body case 201. An internal liquid pipe 205 is connected to the liquid supply pipe connecting portion 202B, and further, the liquid inlet side of the liquid processing nozzle 71 of FIG. 20 is connected via a flow sensor (flow switch) 204 and a pipe joint 203. Is connected to the liquid discharge pipe connecting portion 202A.
A gas supply port joint 211 for connecting a gas supply pipe connected to an external gas supply source is attached to the surface of the main body case 201. The gas introduction joint 30 and the gas supply port joint 211 of the liquid processing nozzle 71 are connected to each other by a gas supply pipe 210. On the way, the check valve 207 and the electromagnetic valve 208 are connected from the liquid processing nozzle 71 side. And the pressure sensor 209 are arranged in this order. The check valve 207 is for preventing a reverse flow of the liquid flow from the liquid processing nozzle 71 side when the gas supply flow in the gas supply pipe 210 is interrupted, and the electromagnetic valve 208 is in the gas supply pipe 210. This is for switching the gas supply flow between the cutoff state and the supply state. The pressure sensor is for detecting the gas pressure in the gas supply pipe 210 to determine the presence or absence of the gas supply flow.
The main body case 201 is further provided with a control board 212 that constitutes a gas supply control means for switching and controlling the power supply circuit 213 and the gas supply flow in the gas supply pipe 210 between a cut-off state and a supply state. A power switch 214 and a power lamp 215 are attached to the surface of the battery. The switch signal SS from the power switch 214 and the detection signals SF and SP from the flow sensor 204 and the pressure sensor 209 are input to the control board 212. An operation signal from the gas flow control operation unit 216 is also input to the control board 212. The power supply circuit 213 receives the drive power supply voltage from the commercial power supply via the power supply cord 217c and the power supply plug 217 (or an AC adapter with a plug), and outputs the drive voltage and signal source voltage of each place to the control board.
The control board 212 performs the following control operation.
(1) As the power switch 202 is turned on, power supply voltage 215 is detected and the power lamp 215 is turned on.
(2) When all of the following conditions a to c are satisfied, the drive signal SVD is output to the solenoid valve 208 to drive the solenoid valve 208 to the open state (thereby supplying gas to the liquid processing nozzle). Gas is supplied through the pipe 210).
a. The flow sensor 204 outputs a detection signal SF for detecting the liquid flow in the internal liquid pipe 205;
b. The pressure sensor 209 outputs a gas supply pressure detection signal Sp in the gas supply pipe 210, and
c. The gas flow control operation unit 216 is in an operation state permitting gas supply.
(3) If any one of a to c in (2) is not established, the electromagnetic valve 208 is kept closed.
A usage example of the gas dissolving apparatus 200 of FIG. 28 and the operation in that case will be described with reference to FIG. Here, the application destination of the gas dissolving apparatus 200 is a hair washing table such as a beauty salon, and a mode in which carbon dioxide gas is used as gas and hot water for washing hair in which the carbon dioxide gas is dissolved is supplied from the shower 401 is taken as an example. The hot and cold water mixing tap 408 of the water heater and the liquid supply pipe connecting portion 202B of the gas dissolving apparatus 200 are connected by water faucet fittings 406 and 407 via an inflow side hose 405 forming a liquid supply pipe. Further, the shower head 401 and the liquid discharge pipe connecting portion 202A of the gas dissolving apparatus 200 are connected to each other by faucet fittings 403 and 404 through an outflow side hose 402 as a discharge pipe. The pressure reducing valve 411 of the carbon dioxide cylinder 410 serving as a gas supply source and the gas supply port joint 211 of the gas dissolving apparatus 200 are connected by a gas supply tube 412.
The gas dissolving apparatus 200 of FIG. 28 operates as follows.
When the power switch 214 is turned on and the valve of the carbon dioxide gas cylinder 411 is open, if the hot-water mixing tap 408 is opened in this state, hot water is supplied to the gas melting apparatus 200 and sprayed from the shower head 401. . At this time, the flow sensor 204 in FIG. 28 detects the flow of hot water, and the pressure sensor 209 detects the carbon dioxide pressure supplied through the gas supply pipe 210. SF and gas supply pressure detection signal SP are input. Therefore, in this state, if the gas flow control operation unit 216 enters an operation state in which the gas supply is permitted, the control board 212 outputs the drive signal SVP to the electromagnetic valve 208, and the electromagnetic valve 208 is opened in response to this, and the hot water is supplied. Carbon dioxide gas is supplied to the flowing liquid processing nozzle 71, and becomes hot water containing dissolved carbon dioxide gas and fine bubbles and is jetted from the shower head 401. On the other hand, if the operation state permitting the gas supply in the gas flow control operation unit 216 is released, the control substrate 212 stops the output of the drive signal SVP, the electromagnetic valve 208 is closed, and the carbon dioxide gas is supplied to the liquid processing nozzle 71. Stops. As a result, hot water containing only fine bubbles due to dissolved air is jetted from the shower head 401.
When water is circulated through the liquid processing nozzle 1 so that the dynamic pressure is 0.1 MPa at the liquid inlet with the liquid outlet side opened, the flow rate of water flowing out from the liquid outlet is defined as Q, and the total flow of the processing core section The water flux Q / St normalized by the cross-sectional area St is 0.5 L · mm. ² Per minute (standard configuration), the dynamic water pressure on the coal liquid inlet side is 0.015 MPa or more and 0.3 MPa or less, and the carbon dioxide / water flow ratio Q1 / Q2 is 0.1 or more and 1. If water and carbon dioxide gas are supplied to the liquid treatment nozzle in one pass with a gas flow rate of 0 or less (however, the gas flow rate is a volumetric flow rate converted to a pressure of 0.1 MPa), the carbon dioxide gas dissolves in water with a dissolution efficiency of 40% or more be able to.
In this embodiment, the gas flow control operation unit 216 is configured as a foot switch, and the state in which the foot switch 216 is urged by the foot is defined as an operation state that permits gas supply (of course, the reverse is also possible). Good). For example, when a hair washing operator such as a hairdresser holds the shower head 401 to wash the hair of a customer or the like, carbon dioxide gas is supplied while the foot switch 216 is stepped on. Gas supply stops immediately. Therefore, the use of the carbonated fine bubble water and the non-carbonated fine bubble water can be quickly and finely switched by operating the foot switch 216.
In the carbonated fine bubble water mode, blood circulation promotion effect by carbon dioxide permeation into the scalp (and the relaxation effect that accompanies it: the so-called head spa effect) can be obtained, and the cuticle of the hair is opened so that moisture can be easily absorbed into the hair. The action is remarkable. Furthermore, when hair dyeing work is performed using an amine-based hair dyeing agent, the hair dyeing agent is washed away with carbonated fine bubble water, so that damage to the hair due to alkali reaction can be reduced by the neutralizing effect of carbonic acid, or , You can enjoy the advantage that even long hair can be dyed uniformly and beautifully. On the other hand, fine bubbles are mainly used for cleaning effects such as removal of sebum, scalp dirt, and horny plugs that fill pores, as well as to improve the moisture retention of the hair and to prevent rough hands by maintaining the skin's moisture retention. It can be enjoyed in any mode of carbonated fine bubble water and non-carbonated fine bubble water. There is also a report that when the sebum stain is particularly strong, the effect of removing sebum is more remarkable when the pH of the warm water is not acidic, that is, non-carbonated fine bubble water. Since the carbonic acid fine bubble water mode naturally involves the consumption of carbon dioxide gas, it is more economical to suppress the carbon dioxide gas consumption by using non-carbonic fine water bubbles in a situation where the above-mentioned effect specific to carbonation is not particularly required. Thus, it can be said that it is desirable to appropriately use each mode of the carbonated fine bubble water and the non-carbonated fine bubble water depending on the scene.
Next, when the hot and cold water mixing tap 408 is closed in FIG. 29, the electromagnetic valve 208 in FIG. 28 automatically closes, and even if the valve of the carbon dioxide cylinder 410 is open, useless carbon dioxide may flow out of the shower head 401. Absent. When the carbon dioxide gas cylinder 410 becomes empty, the pressure sensor 209 detects a gas pressure drop and similarly closes the electromagnetic valve 208. Thereby, even when the use of hot water is continued in the non-carbonated fine bubble water mode, there is no concern that water flows backward to the carbon dioxide cylinder 410 side via the gas supply pipe 210. The check valve 207 should also act to prevent the backflow of water, but many of the check valve type commercially available gas check valves cannot often stop the backflow of low-pressure liquid. It is effective to reliably prevent backflow using
(Embodiment 4)
The gas dissolving device 260 in FIG. 30 shows an example in which the liquid flowing out from the liquid processing nozzle is returned to the nozzle via the pump and circulated while circulating, and FIG. 31 shows an example of its use. It is shown. The multiphase flow supply means (specifically, the liquid supply unit) includes circulation pipes 422 and 425 that return from the liquid storage unit 430 that stores the liquid to the liquid storage unit 430 via the liquid processing nozzle 71 (FIG. 30), The liquid in the liquid storage unit 430 is mixed with the gas from the gas supply unit 410 through the circulation pipes 422 and 425, and then circulated through the liquid processing nozzle 71 (FIG. 30) and then returned to the liquid storage unit 430. The liquid feed pump 218 is configured to be liquid.
Returning to FIG. 30, the configuration of the gas dissolving apparatus 260 will be further described. Since the gas dissolving device 260 has the same configuration as the gas dissolving device 200 of FIG. 28 except that the liquid feed pump 218 is incorporated in the middle of the internal liquid pipe 205, only the differences will be mainly described below. Explanation will be given, and the same components as those in FIG. That is, in this configuration, the internal liquid pipe 205 is divided into a first pipe 205A on the pump inlet side and a second pipe 205B on the pump outlet side, which are connected to the suction side and the discharge side of the liquid feed pump 218, respectively. The liquid feed pump 218 receives a drive voltage from the power supply circuit 213.
28 is omitted, and the control board 212 performs the following control operation.
(1) As the power switch 202 is turned on, power supply voltage 215 is detected and the power lamp 215 is turned on.
(2) When both of the following conditions a and b are satisfied, a drive signal SVD is output to the solenoid valve 208 to drive the solenoid valve 208 to the open state (thereby supplying gas to the liquid processing nozzle). Gas is supplied through the pipe 210).
a. The flow sensor 204 outputs a detection signal SF for detecting the liquid flow in the internal liquid pipe 205;
b. The pressure sensor 209 outputs a gas supply pressure detection signal Sp in the gas supply pipe 210, and
(3) When either a or b in (2) is not established, the electromagnetic valve 208 is kept closed.
A usage example of the gas dissolving apparatus 260 of FIG. 30 will be described with reference to FIG. 31 together with the operation in that case. The application destination of the gas dissolving device 260 is a bath, and it is used as a so-called carbonated bath in which carbon dioxide gas is dissolved as a gas while circulating the hot water in the bathtub 430 as a liquid storage unit by the gas dissolving device 260. . Connected to the liquid supply pipe connecting portion 202B of the gas dissolving apparatus 260 is a return side pipe 425 that forms part of the above-described circulation pipe that returns the hot water in the bathtub 430 to the gas dissolving apparatus 260. The liquid discharge pipe connection 202A of the gas dissolving device 260 is connected to a discharge side pipe 422 that forms part of a circulation pipe that discharges hot water in which gas has been dissolved by the gas dissolving device 260 into the bathtub 430. ing. The pressure reducing valve 411 of the carbon dioxide cylinder 410 serving as a gas supply source and the gas supply port joint 211 of the gas dissolving device 260 are connected by a gas supply tube 412.
In FIG. 31, first, hot water is filled in a bathtub 430 from a water heater (not shown). Then, the valve of the carbon dioxide cylinder 411 is opened, and the power switch 214 (FIG. 30) is turned on. Then, the pump 218 starts to operate, sucks hot water in the bathtub 430 through the return side pipe 425, and circulates and flows so as to return to the bathtub 430 through the discharge side pipe 422 while passing through the liquid processing nozzle 71. At this time, in FIG. 30, the flow sensor 204 detects the flow of hot water, and the pressure sensor 209 detects the carbon dioxide pressure supplied through the gas supply pipe 210. A detection signal SF and a gas supply pressure detection signal Sp are input. Therefore, the control board 212 outputs the drive signal SVP to the solenoid valve 208, the solenoid valve 208 is opened, the carbon dioxide gas is supplied to the liquid processing nozzle 71, and circulates as hot water containing dissolved carbon dioxide gas and fine bubbles. Will continue. As shown in FIG. 31, since the circulation is performed while the supply of the carbon dioxide gas is continued, the carbon dioxide gas concentration in the hot water in the bathtub 430 increases with the passage of the circulation time. Then, when the power switch 214 is turned off at the preferred carbon dioxide concentration, the circulation is stopped. Then, even if the electromagnetic valve 208 in FIG. 26 is automatically closed and the valve of the carbon dioxide cylinder 410 is open, there is no possibility that wasteful carbon dioxide will be lost.
As is well known, when bathing in this state, when carbon dioxide is used, a blood circulation promoting effect by carbon dioxide permeation into the skin can be obtained. However, by containing a large amount of fine bubbles, the effect of improving the moisture retention of the skin and removing dirt is also achieved. In addition, since carbon dioxide is contained as fine bubbles, there is an advantage that the concentration of dissolved carbon dioxide lasts for a long time even after the circulation by the apparatus 260 is stopped.
On the other hand, when the carbon dioxide cylinder 410 becomes empty or the valve of the carbon dioxide cylinder 410 is closed, a gas pressure drop is detected by the pressure sensor 209 and the electromagnetic valve 208 is similarly closed. At this time, if the power switch 214 is turned on, the hot water in the bathtub 430 is circulated in a state where the carbon dioxide gas is not supplied. In this case, the hot water in the bathtub 430 becomes water containing fine bubbles. If a hydrogen cylinder 420 is used instead of the carbon dioxide cylinder 410, it can be used as a hydrogen bath.
(Embodiment 4)
FIG. 32 shows an example of an apparatus in which nitrogen or oxygen is dissolved in a liquid while circulating using the liquid processing nozzle of the present invention. In the apparatus 550, raw water (including an aqueous solution and a colloidal solution) 502 is stored in a tank 501, and a gas introduced by an ejector or the like is provided in the raw water supply pipe 51 extending from the tank 501. The unit 219, the liquid feed pump 505, and the liquid processing nozzle 1 of FIG. 1 (the liquid processing nozzle 151 of FIG. 13 and the liquid processing nozzle 51 of FIG. 18 may be provided) in this order. Nitrogen gas is supplied to the gas introduction unit 219 from a nitrogen cylinder 430 as a gas supply source via a pressure reducing valve 411 and a gas supply tube 412. A pipe 507 extending from the tank 501 is formed as a circulation pipe that returns from the tank-side outlet 506 to the tank-side inlet 508 via the gas introduction unit 219, the liquid feed pump 505, and the liquid processing nozzle 1.
When the liquid feed pump 505 is operated, the raw material water from the tank 501 is supplied with nitrogen gas from the nitrogen cylinder 430 at the gas introduction unit 219 and becomes a mixed phase flow of water / nitrogen gas, and the liquid feed pump 505 generates the nitrogen gas phase. After preliminary pulverization, the liquid processing nozzle 1 dissolves the nitrogen gas and pulverizes it into fine bubbles, and returns to the tank 502. Thereafter, while the water 502 in the tank is circulated, the nitrogen gas is continuously dissolved and pulverized into fine bubbles, so that the dissolved concentration of nitrogen gas or the formation concentration of fine bubbles is increased. The circulating water thus obtained is recovered from an outlet 503 having a valve 504 provided in the tank. As a result, the raw material water 502 can be dissolved in nitrogen, and thus deoxygenated. By increasing the dissolution efficiency of nitrogen gas, the oxygen concentration of the raw water 502 can be reduced with a smaller nitrogen gas flow rate and circulation time.
Further, if the circulation is continued while supplying nitrogen gas even after the nitrogen concentration reaches the saturation value, the dissolved nitrogen concentration reaches a peak, but the formation concentration of fine bubbles continues to increase. As a result, there is no significant difference in the dissolved nitrogen concentration itself compared to water in which nitrogen gas is dissolved only by pressurization, for example. The duration of the dissolved nitrogen concentration is considerably longer than that of water in which nitrogen gas is merely dissolved due to the large amount of fine bubble nitrogen (nitrogen nanobubbles or colloidal nitrogen). As a result, a low dissolved oxygen concentration state can be maintained for a long time. Since the liquid processing nozzle 1 has the above-described standard configuration, the pump water pressure on the inlet side of the liquid processing nozzle 1 is, for example, 0.015 MPa or more and 0.3 MPa or less, and the nitrogen / water flow rate ratio Q1 / Q2 is set to 0.00. The concentration of dissolved oxygen in water can be 1 ppm or less, for example, from 1 to 0.3, for example, up to about 3 cycles. By introducing such oxygen-reduced water into the cleaning of the produced food (particularly a vegetable washer), oxidation is suppressed by oxygen, which greatly contributes to improving the freshness of the food to be cleaned. In addition, ice obtained by freezing oxygen-reduced water is called nitrogen ice, and when used for low-temperature storage of fresh fish or the like, it also exerts great power in maintaining its freshness. Further, the raw water 502 can be an alcoholic beverage such as liquor or wine. As a result, oxygen dissolved before circulation is discharged by nitrogen substitution, and the alcohol beverage can be prevented from being oxidized. Thereby, it becomes possible to reduce or abolish the addition amount of antioxidants such as nitrite that have been added to the antioxidant of beverages. As a result of the introduction of a large amount of nitrogen fine bubbles, the oxygen concentration in the alcoholic beverage is less likely to increase thereafter, and long-term quality maintenance is possible. Note that hydrogen can be used instead of nitrogen.
In FIG. 32, when an oxygen cylinder 440 is used instead of the nitrogen cylinder 430, the raw water 502 can be dissolved in oxygen. The dissolved oxygen concentration can be significantly increased with a small oxygen gas flow rate and circulation time. In place of the tank 501, it can be used as a fish breeding tank or a ginger for curing live fish (including shellfish), and even if oxygen consumers such as fish and shellfish are present, the oxygen gas flow rate can be reduced. Highly dissolved oxygen concentration can be maintained, which in turn contributes greatly to maintaining the freshness of fish and shellfish, or improving rearing density. As the gas, pure oxygen may be used, or when using raw water deficient in oxygen from the beginning, a mixed gas of nitrogen and oxygen such as air may be used. When a liquid processing nozzle having a standard configuration is used, when the oxygen flow rate for forming the multiphase flow having the above-described configuration is Q1 and the water flow rate is Q2, the pump water supply pressure on the inlet side of the liquid processing nozzle 1 is set to 0. By circulating and supplying 015 MPa to 0.3 MPa and an oxygen / water flow rate ratio Q1 / Q2 of 0.1 to 0.3, the dissolved oxygen concentration of water can be increased to 10 ppm to 40 ppm. In addition to the cylinder, the oxygen gas source or the nitrogen gas source may be a PSA (Pressure Swing Adsorption) type oxygen concentrator or a nitrogen concentrator, or a liquid for large-scale gas dissolution. It is also possible to use a vaporized gas generator using oxygen or liquid nitrogen.
The apparatus 560 of FIG. 33 is a modification of the apparatus of FIG. 32 so as to be able to circulate and dissolve ozone (the same reference numerals are given to parts common to the apparatus 550 of FIG. 32, and description thereof is omitted). ). First, as an ozone generation source, a source of oxygen gas as a raw material, here, an oxygen cylinder 440 and an ozone generator (ozonizer) 563 that ozonizes oxygen from the oxygen cylinder are provided, and a gas supply tube 412 is provided. Is supplied from an ozone generator 563 with, for example, an ozone-containing gas having a concentration of 10 ppm to 100 ppm (oxygen that has not been ozonized except for ozone). By performing the circulation treatment in the same manner as in FIG. 32, the raw water can be made into ozone water containing fine bubbles of ozone / oxygen mixture. In the case of using a liquid processing nozzle having a standard configuration, when the ozone flow rate for forming the multiphase flow having the above-described configuration is Q1 and the water flow rate is Q2, the pump water supply pressure on the inlet side of the liquid processing nozzle 1 is 0. By circulating and supplying the ozone-containing gas / water flow ratio Q1 / Q2 between 0.1 and 0.3 MPa in the range of 0.1 to 0.3 MPa, the dissolved ozone concentration of water is, for example, 1 ppm or more (although there is no limit on the upper limit). For example, 20 ppm or less). Since most of the gas phase in the gas-liquid mixed phase flow to be circulated is oxygen, the waste oxygen / ozone mixture (hereinafter referred to as waste ozone gas) that has not dissolved floats in the tank 501. Therefore, in this embodiment, a waste ozone gas return path 413 is provided to return the recycled waste ozone gas to the ozone generator and reuse it, thereby effectively utilizing oxygen and ozone. Note that air can also be used as the oxygen source.
It is known that dissolved ozone water generally disappears in about several minutes, for example, about 5 ppm due to decomposition of ozone when exposed to the atmosphere (particularly under ultraviolet irradiation). However, when the method of the present invention is used, even when ozone is dissolved, the resulting ozone water contains a large amount of fine bubbles containing ozone. Thereby, the duration of the dissolved ozone concentration when exposed to the atmosphere can be dramatically increased.
(Embodiment 5)
When carbon dioxide is dissolved, an aqueous sodium hypochlorite solution can be used as water. As a result, the pH value of the aqueous sodium hypochlorite solution is maintained at a weak acidity of, for example, about 4.3 to 6, and the concentration of hypochlorous acid in a dissociated state effective for sterilization and disinfection can be greatly increased. The fluctuation in pH value can be reduced by the pH buffering action unique to carbonic acid. The sodium hypochlorite aqueous solution has a hypochlorite ion concentration of 10 ppm or more and 1000 ppm or less (particularly preferably 30 ppm to 200 ppm or less), and a dissolved concentration of carbon dioxide gas is 200 ppm or more and 1500 ppm or less.
For example, a sodium hypochlorite aqueous solution having a target concentration is prepared in advance, stored in a tank or the like (not shown), and sent from the liquid inflow pipe connecting portion 202B side of the gas dissolving device 200 of FIG. 28 using an external pump or the like. The solution is dissolved to dissolve carbon dioxide gas, and the pH of the sodium hypochlorite aqueous solution is adjusted to 4.3 to 6, and then taken out from the liquid discharge pipe connecting portion 202A side and used for disinfection.
On the other hand, without using the sodium hypochlorite aqueous solution, the carbon dioxide gas may be dissolved in normal water using the gas dissolving apparatus 200 of FIG. 28, and the sodium hypochlorite aqueous solution may be added later. If it does in this way, especially the chemical-resistance required for the material of the collision part (screw member) of a liquid processing nozzle can be reduced significantly. In this case, a sodium hypochlorite aqueous solution whose pH has been adjusted by adding a sodium hypochlorite aqueous solution having a concentration higher than the target concentration to the water in which the carbon dioxide gas is dissolved, taken out from the liquid discharge pipe connecting portion 202A side. Can be used.
On the other hand, an apparatus incorporating a sodium hypochlorite aqueous solution supply unit for quantitatively supplying a sodium hypochlorite aqueous solution to water in which carbon dioxide gas delivered from the liquid processing nozzle is dissolved in the gas dissolving device 260 of FIG. It is also possible to configure. An apparatus 270 in FIG. 34 shows an example, and a sodium hypochlorite aqueous solution supply unit 310 includes an aqueous solution tank 311 for holding a sodium hypochlorite aqueous solution and an aqueous solution incorporated downstream of the liquid processing nozzle 71. A supply nozzle 317 and a liquid feed pump 312 for quantitatively feeding the sodium hypochlorite aqueous solution in the aqueous solution tank 311 to the aqueous solution supply nozzle 317 are provided. In this embodiment, the aqueous solution supply nozzle 317 is configured by using a tee joint (which may be a venturi-type ejector), a liquid introduction joint 330 is attached to the branch opening, and the liquid supply pipe 314 from the aqueous solution tank 311 is fed. It is attached to a liquid introduction joint 330 via a liquid pump 312. The rest of the configuration and basic operation are the same as in FIG. 28, and the same reference numerals as in FIG. 26 are assigned to the common components.
When the power switch 214 is turned on, the pump 218 operates, and the carbon dioxide gas is dissolved by the liquid processing nozzle 71 in the same operation as in FIG. 29 while taking the raw water from the liquid inflow pipe connecting portion 202B side. At the same time, the liquid feed pump 312 operates, and a sodium hypochlorite aqueous solution is quantitatively injected from the aqueous solution supply nozzle 317 downstream of the liquid processing nozzle 71. The flow rate of the liquid feed pump 312 depends on the concentration of the sodium hypochlorite aqueous solution to be added and the flow rate of the raw material water fed by the pump 218, and the hypochlorite ion concentration obtained on the liquid discharge pipe connecting portion 202A side is It is set to be 10 ppm or more and 1000 ppm or less.
It is also possible to configure so that the supply / stop of carbon dioxide gas can be switched manually or automatically during the injection of the sodium hypochlorite aqueous solution. In FIG. 35, as indicated by a two-dot chain line, a changeover switch 331 is added, and the control board 201 receiving the changeover signal Sc opens and closes the electromagnetic valve 208 in the same manner as the operation of the foot switch 216 in the apparatus 200 of FIG. Switch between carbon dioxide supply and stop. In this manner, weakly acidic hypochlorous acid water having a high sterilization property is obtained from the liquid discharge pipe connecting portion 202A in the carbon dioxide gas supply mode, and alkaline hypochlorous acid having a high detergency in the carbon dioxide gas stop mode. A sodium aqueous solution (that is, a solution obtained by simply diluting the sodium hypochlorite water in the tank 311 with the raw water supplied by the pump 218) is obtained. For example, using an alkaline sodium hypochlorite aqueous solution obtained in the carbon dioxide gas stop mode, after first cleaning and removing oils and fats and protein stains, the mode is switched to the carbon dioxide gas supply mode to weakly acidic hypochlorous acid. It can contribute to the maintenance of a higher level of hygiene, such as sterilization with water.

Hereinafter, various tests were performed to confirm the effect of the liquid treatment nozzle of the present invention.
(Example 1)
As the nozzle configuration, the nozzle 1 shown in FIG. 1 was used for the test in which gas was not dissolved, and the nozzle 171 (FIG. 26) shown in FIG. 1 was used for the test in which gas was dissolved. The gas introduction hole 28 has an inner diameter of φ2 mm. The material of the nozzle body 2 is ABS resin, the inner diameter of the liquid inlet 4 and the liquid outlet 5 is φ14 mm, and the lengths of the inflow chamber 6 and the outflow chamber 7 in the flow direction are 30 mm. Regarding the core part CORE, the length of the throttle hole 9 was set to 5.3 mm, and the inner diameter D of the throttle hole 9 was set to various values of φ2.1 to φ8.0 mm.
The screw members were arranged in the form shown in FIG. 2 (Tables 3 to 6) and in the form shown in FIG. 6 (Tables 1 and 2: However, no liquid flow gap was formed). All of the screw members were of various dimensions having a screw outer diameter of M1.0 to M2.0 and a thread valley depth of 0.25 to 0.4 mm. The total flow cross-sectional area St was set to various values of 1.23 to 40.27 mm ² in combination with the throttle hole inner diameter D. Then, a photograph image of the screw layout in the aperture hole as shown in FIG. 3 and FIG. 7 is taken, and the total distribution cross section St is calculated based on the number of pixels in the distribution region, and the valley point is referenced on the image. Counted separately inside and outside the circle. The total valley score is Nt, and the 70% valley score inside the reference circle is N ₇₀ .
Total flow cross-sectional area St, liquid flow gap cross-sectional area Sc, 70% cross-sectional area S ₇₀ (portion located inside reference circle C ₇₀ of total flow cross-sectional area St), 70% cross-sectional ratio σ ₇₀ (≡S ₇₀ / St), thread valley depth correction coefficient α based on the aforementioned equation (1), corrected total valley score (α · Nt), corrected 70% valley score (α · N ₇₀ and α · N _{(σ 70/50) · N} 70), corrected to 70% Hotani number _{(≡α · (Nt-N 70} ) · 0.38 = α · 0.38Nc 70)) and the effective valley points Ne (≡α · represents the value of _{(0.38Nc 70 + (σ 70/} 50) · N 70) are summarized in tables 1 to 6. the value of the dimensions or parameters granted in the table * are outside the scope of the present invention It shows that it is.

The following tests were performed using the nozzle.
(1) Measurement of flow rate at a constant water pressure A pipe extending from a water tap with a source pressure of 0.2 MPa was connected to the inlet side of each nozzle, and a water pressure gauge was attached to the inlet side. In this state, the opening of the water tap is adjusted so that the indicated pressure of the water pressure gauge becomes 0.1 MPa, and the flow rate of water (dissolved oxygen concentration: 8 ppm) flowing out from the outlet of the nozzle (water flow rate Q: L / min) was measured. The results are shown in Tables 1 to 6 together with the value Ne / Q obtained by dividing the number of effective valley points Ne by the flow rate Q.
(2) Measurement of average bubble diameter In (1), tap water flowing out from the nozzle outlet is led to a measurement cell of a laser diffraction particle size distribution measuring device (Shimadzu Corporation: SALD7100H), and the average bubble diameter is determined. It was measured. The water flowing out from the nozzle is collected in a 1 L beaker and then left for 1 minute to float coarse bubbles and then used for measurement. The laser diffraction particle size distribution measuring device makes a laser light beam incident on a measurement cell at a certain angle, and a three-dimensional scattering distribution of light scattering generated at the gas-liquid interface according to the refractive index difference between the bubble and water and the bubble diameter. By utilizing the difference, scattered light intensity for each angle is detected by an individual photodetector, and information related to the bubble diameter distribution is obtained from the detected intensity distribution of each sensor. The obtained distribution is a volume bubble size distribution, but the software attached to the apparatus converts the bubble into a spherical shape by converting it into a spherical shape, and the number average bubble size calculated based on this is displayed. Further, the measuring device is accompanied by a function for measuring the absorbance of the laser light passing through the cell, and the higher the absorbance, the higher the concentration of bubbles in the cell. The absorbance value is a relative value, and information on the absolute value of the bubble concentration cannot be obtained. However, it is possible to relatively compare the bubble concentrations of a plurality of samples to be measured simultaneously. The absorbance value is also displayed together (note that the maximum absorbance displayed by the device is 0.2).
(3) Measurement of moisture absorption and evaporation behavior of hair Using human white hair (100%) (BS-C, manufactured by Beaulux Co., Ltd.) as a hair sample for evaluation, prepared a bundle of hair samples 2g. did. In (1), tap water flowing out from the outlet of the nozzle was placed in a 500 cc beaker, and the hair sample was dipped well and held for 10 minutes. Next, the sample was taken out, blotted with towel paper, and then dried with a commercially available dryer for 1 minute so that no moisture was felt on the fingertips. Each dried sample was sealed and stored in a plastic bag with a double chuck. The hair sample thus prepared was subjected to moisture evaporation behavior measurement by the heating weight loss method. Specifically, 2 g of each sample cut to a length of 3 cm was weighed and set in a chamber of a commercially available thermobalance device (manufactured by Shimadzu Corporation). Next, the temperature in the chamber was raised to 80 ° C. and held for 15 to 30 minutes, and the change in weight was measured at 1 minute intervals. After confirming that the weight loss became almost constant, the temperature in the chamber was raised to 120 ° C., and held for another 10 minutes, and the change in weight was measured at 1 minute intervals. From this weight change curve, the weight ratio of free water and bound water in the hair was calculated by the method described later.
(4) Carbon dioxide dissolution test Various nozzles shown in Table 1 were incorporated as the nozzles 71 of the gas dissolution apparatus 200 of FIG. 28, and hot water having a water temperature of 35 ° C. was attached to the liquid supply pipe connection 202B side using a water heater. Supply the carbon dioxide gas from the gas supply port joint 211 so that the dynamic water pressure is adjusted to 0.1 MPa so that the supply pressure is 0.2 MPa and the carbon dioxide gas flow rate is 70% of the water flow rate. Thus, carbon dioxide gas was dissolved and the hot water was collected from the hose connected to the liquid outflow pipe connecting portion 202A, and the carbon dioxide concentration was measured using a commercially available carbon dioxide concentration meter.
(5) Nitrogen gas dissolution test Various nozzles shown in Table 1 (but no gas introduction holes) are incorporated in the apparatus 550 shown in FIG. 32, and the tank 501 is filled with 30 L of tap water (dissolved oxygen concentration 8 ppm) and pump circulation. The flow rate was adjusted so that the supply pressure measured between the nozzle 1 and the pump 505 was 0.1 MPa. In this state, nitrogen gas is supplied from the gas introduction part 219 while adjusting the supply pressure to 0.3 MPa and the nitrogen gas flow rate to be 20% of the circulation flow rate in terms of normal pressure to dissolve the nitrogen gas, and the tank The dissolved oxygen concentration in the water was continuously measured with an optical dissolved oxygen meter, and the time required for the oxygen concentration to become less than 1 ppm was specified.
(6) Oxygen gas dissolution test Various nozzles (but no gas introduction holes) shown in Table 1 are incorporated in the apparatus 550 shown in FIG. 32, and the tank 501 is filled with 30 L of water deoxygenated by a known vacuum degassing process. The pump circulation flow rate was adjusted so that the supply pressure measured between the nozzle 1 and the pump 505 was 0.1 MPa. In this state, pure oxygen gas was supplied from the gas introduction part 219 while adjusting the supply pressure to 0.3 MPa and the oxygen gas flow rate to be 20% of the circulation flow rate in terms of normal pressure, thereby dissolving oxygen gas. The circulation time was determined to be equal to the time obtained by dividing the volume of purified water in the tank by the pump circulation flow rate. After the circulation was stopped, 5 L of water dissolved with oxygen gas was immediately taken from a outlet 503 into a resin beaker having an opening diameter of 18 cm, and dissolved oxygen was measured with an optical dissolved oxygen meter.
Hereinafter, the obtained results will be described.
(A) About the generation efficiency of fine bubbles For each nozzle in Tables 1 to 6, the effective valley point density Ne / St, even if the outer diameter and depth of the screw, the cross-sectional area of the throttle hole, etc. are variously set. When in association with values to organize the measurement results of the micro-bubbles, for the nozzles which the value of Ne / St is ensured 1.5 / mm ² or more, the following can be found.
・ The average number of bubbles measured by a laser scattering particle size meter is very small, approximately 200 nm or less.
-Compared with the Ne / St value of less than 1.5 / mm ^2, the absorbance value reflecting the concentration of fine bubbles is increased without exception, and the fine bubble generation efficiency is excellent. it is obvious.
For the nozzles having the screw arrangement of FIG. 7 shown in Table 1 and Table 2, the inner diameter D of the liquid flow path is set to approximately 2 mm to 4.5 mm (preferably 2 mm to 3.5 mm), and all While setting the flow sectional area St to 1.2 mm ^{2 to} 10 mm ² (preferably 1.2 mm ^{2 to} 5 mm ² ), the outer diameter of the screw member is M1.2 to M1.6, and the valley depth is 0.25 mm. When the value is selected to be 0.35 mm or less, the value of the effective valley point density is remarkably increased, and it can be seen that better fine bubble generation efficiency can be achieved. On the other hand, for the nozzles having the screw arrangement of FIG. 4 shown in Tables 3 to 6, the inner diameter D of the liquid flow path is set to about 2.5 mm to 7 mm (preferably 2.9 mm to 5.5 mm). , While setting the total flow sectional area St to 2.5 mm ^{2 to} 35 mm ² (preferably 4 mm ^{2 to} 13 mm ² ), the outer diameter of the screw member is M1.2 to M1.6, and the valley depth is 0.25 mm. When the value is selected to be 0.35 mm or less, the value of the effective valley point density Ne is remarkably increased, and better microbubble generation efficiency can be achieved. It is clear that the fine bubble generation efficiency at a large flow rate is improved as compared with the nozzle of FIG.
(B) Moisture absorption and evaporation behavior of hair Among the treated waters from the nozzles of Tables 1 to 6, as representative ones, the numbers 106 (Example: effective valley density 2.8) and 107 in Table 4 FIG. 35 shows a weight loss curve associated with moisture evaporation of the hair sample for (Example: effective valley point density 2.2) and No. 110 (comparative example: effective valley point density 1.2). FIG. 36 to FIG. 38 individually show the weight reduction curves of the respective nozzles. It can be seen that the rate of water evaporation is clearly slower as the water is treated with a nozzle having a higher effective valley point density.
The form of the weight reduction curve reflects the binding state between the protein polymer constituting the hair and water. This will be described in detail below. For example, when hot water obtained from the nozzle is sprayed from a shower and subjected to hair washing, the water treated by the nozzle having a higher effective valley point density increases the water permeability to the hair and skin, and the drying speed of the hair after washing It is known that there are very many subjects who feel that the improvement is achieved. It seems that this tendency cannot be explained only by the effect of microbubbles in the water. Specifically, from the measurement results of microbubbles, it is certain that the water contains a large amount of microbubbles in the nano range, but the physical properties of water, especially the population of water that is polarized molecules, It is thought that nanobubbles are involved in target (statistical) behavior, and the water penetration ability may increase.
When the moisture retained in proteins such as wet hair and egg white is kept at a constant temperature below the boiling point of water to evaporate the moisture, the rate of weight loss associated with the evaporation of the moisture is not constant. It is known to exhibit a behavior following a characteristic cusp-shaped curve in which the rate of weight reduction gradually decreases. If the evaporation behavior of the moisture contained in the hair is governed by the diffusion of water molecules in the radial direction of the hair, the weight reduction curve should have a smooth curve shape according to the compensation function. However, as shown in FIGS. 36 to 38, the weight reduction curve actually obtained by the measurement includes a straight section where the evaporation rate becomes substantially constant with time. This means that some interaction between water molecules and hair molecules that are not diffusing controls the evaporation behavior within the hair, and evaporates in the interval where the weight loss rate is low, which evaporates in the final stage. It means that the more water is, the more the evaporation is inhibited by the interaction with protein molecules.
Specifically, water contained in wet hair is classified into the following types, and it is known that the evaporation rate increases in this order.
1) Bulk water Water that is macroscopically and physically held outside the protein polymer structure that constitutes hair, and that has little influence on the interaction with the protein polymer that constitutes hair. It is the water held in the space between the hairs and the irregularities of the cuticles on the hair surface, and it is considered that the group size of water molecules statistically grasped is relatively large.
2) Free water Although it is taken into the polymer structure, the influence of the interaction with the polymer is small, and the group size of water molecules is almost the same as that of bulk water and is held in the hair. Water. It is considered to be in a state of being substantially close to bulk water.
Bulk water and free water are moisture that makes you feel that your hair is wet when you touch it with your hand. Bulk water is in the form of water droplets, and water that is absorbed by towel paper during sample preparation. Is the amount of moisture that evaporates from the hair until it no longer feels wet when it is dried with a dryer, in other words, when the subject feels that the hair has dried appropriately and finishes drying the dryer. It is thought that.
3) Constrained water Water that is approached to the region where the intermolecular force interaction is strongly applied to the protein polymer chain, and the loose collective bond of water molecules is released by the interaction and retained. For this water to evaporate, it is necessary for the water molecules to move overcoming the intermolecular force with the protein polymer chain, and the evaporation rate is significantly lower than that of free water.
4) Antifreeze water Water bound to strong countries by hydrogen bonds to protein polymer chains. The hydrogen atom contained in the water molecule is positively polarized and charged with a force much higher than the intermolecular force against the protein polymer chain. That is, the water molecules constituting the antifreeze water are in a semi-chemically integrated state with respect to the protein polymer chain, and therefore do not evaporate at a temperature below the boiling point of water.
Bound water penetrates deep into the protein structure and controls various factors such as appearance and feel that create a good hair condition, such as moisture, gloss, softness, suppleness, and the way of hands and brushes. It is thought that there is. The method for estimating the presence and content of water in the protein as described above from the weight loss curve accompanying water evaporation retained by the protein has been proposed in Non-Patent Document 1 for a long time. Cited by various studies, it has become an important tool in investigating the relationship between the mechanical properties of proteins (such as hardness) and the water content.
The weight reduction curve in FIG. 36 will be described as an example. At the initial stage of evaporation, a straight section with a different gradient appears as the bulk water and then free water evaporate, and then the weight reduction rate decreases to correspond to bound water. (For bulk water, a considerable amount is lost due to wiping with towel paper and evaporation during setting to the measuring machine, and often does not appear on the curve). Then, after the weight loss due to holding at 80 ° C. is almost balanced, if the temperature is raised to 120 ° C., a step-like weight loss accompanying evaporation of the antifreeze water appears. Since the bound water is considered to evaporate at the same rate as that in the straight section of the bound water during the free water evaporation period, the weight content of free water and bound water is zero for each straight section. It can be calculated as the difference of the weight axis intercept extrapolated to.
36 to 38 also show the results of calculating the contents of bound water and free water in the hair from the weight reduction curves at each nozzle. Tables 1 to 6 show the weight content (Wb, Wf) of the bound water and free water calculated for the treated water of each nozzle and the value of the total Wb + Wf. From this result, it can be understood that the weight ratio of the bound water when it is applied to the hair increases as the treated water is produced by the nozzle having a higher effective valley point density. Also, it should be noted that when the hair is wet with water, the total weight content of bound water and free water is constant between about 25-30% regardless of the effective valley point density of the nozzle used. It is that you are. This means that the amount of water penetrating into the hair is almost constant, but water treated with the present invention so as to increase the generation efficiency of fine bubbles in particular increases the amount of water converted to bound water. is doing. This also means that the amount of free water that creates the feeling of “wetting” is reduced, which is consistent with the body sensation of the subject who feels that the drying time can be shortened when drying the dryer. Conventionally, it has been considered that the improvement in the moisture retention of the hair is brought about by an increase in the absolute amount of moisture penetrating into the hair. However, in the nozzle of the present invention in which the effective valley point density of the nozzle is secured to 1.5 pieces / mm ² or more, the bound water weight grasped by the above measurement rather than the absolute amount of moisture penetrating into the hair, that is, the hair It is apparent that there is a clear new effect that the amount of water penetrating to the deep part of the three-dimensional structure of the protein molecules constituting is increased.
(C) Gas Dissolution Efficiency From the results of Tables 1 to 6, it can be seen that the higher the effective valley point density Ne, the higher the carbon dioxide gas concentration and the dissolved oxygen concentration, and the better the gas dissolution capacity. In the case of nitrogen, it can be seen that the time until the dissolved oxygen concentration reaches 1 ppm is shorter as the nozzle having a larger effective valley point density Ne, and the deoxygenation ability by nitrogen substitution is improved.

1, 51, 71, 171 Liquid treatment nozzle 2 Nozzle body O Center axis 3 Liquid flow path 4 Liquid inlet 5 Liquid outlet 6 Inflow chamber 7 Outflow chamber 8 Partition portion 9 Restriction hole 10 Colliding portion (screw member)
CORE processing core part 11 mountain part 12 valley part 15 liquid distribution gap 16 inflow side connection part (screw part)
17 Outflow side connection (screw)
20 circumscribed circle 28 gas introduction hole 200,260,270,500,550,560 gas dissolving apparatus

Claims (18)

1. A nozzle body in which a liquid channel having a liquid inlet at one end and a liquid outlet at the other end is formed;
   A processing core portion having a collision portion that protrudes from the inner surface of the liquid flow path and has a plurality of alternating crest portions and trough portions that become high flow velocity portions on the outer peripheral surface;
   In the projection onto the plane orthogonal to the central axis of the liquid channel, the entire area inside the outer peripheral edge of the projection region of the liquid channel in the processing core unit is S1, and the projection region area of the collision unit is S2. The total distribution cross section St of the processing core part is
   St = S1-S2 (unit: mm ² )
   When defined as the cross-sectional area of the liquid inlet and the liquid outlet is set larger than the total flow cross-sectional area St,
   The depth h of the valley portion appearing in the projected outline of the collision portion is secured to 0.2 mm or more, and the liquid centering on the projection point of the central axis among the valley points representing the bottom position of the valley portion. N ₇₀ (pieces) is located inside the reference circle drawn with a radius corresponding to 70% of the distance to the inner periphery of the flow path, and Nc ₇₀ (pieces) is located outside the reference circle. ), And when the valley depth correction coefficient α is h ≧ 0.35 mm, α = 1.
   When h <0.35 mm, α = −60h ² + 41h−6
   As
   70% cross-sectional ratio σ ₇₀ , where S ₇₀ (unit: mm ² ) is the area of the portion located inside the reference circle in the total flow cross-sectional area in the projection.
   σ ₇₀ = S ₇₀ / St × 100 (%)
   As stated, the effective valley points _{Ne Ne = α · (0.38Nc 70} + (σ 70/50) · N 70)
   When defined as
   Liquid processing nozzle effective valley points density expressed by Ne / St is characterized by comprising reserved 1.5 / mm ² or more.
2. The cross-sectional shape of the liquid flow path in the processing core part is a circular shape having an inner diameter D of 2 mm or more and 7 mm or less, and the collision part is set such that the depth of the valley part is 0.2 mm or more and 0.4 mm or less. The liquid processing nozzle according to claim 1, wherein the flow sectional area St is set to 1.2 mm ² or more and 35 mm ² or less.
3. 3. The liquid processing nozzle according to claim 2, wherein the collision part is a screw member having a JIS coarse pitch with an outer diameter M of 1.0 mm or more and 2.0 mm or less.
4. The collision portion is arranged so as to cross the diameter direction in the cross section of the flow path, the inner diameter D of the liquid flow path is set to 2 mm to 4.5 mm, and the total flow cross section St is 1.2 mm ² or more. The liquid processing nozzle according to claim 3, which is set to 10 mm ² or less.
5. Four collision parts are arranged in a cross shape surrounding the central axis in the projection, the inner diameter D of the liquid flow path is set to 2.5 mm or more and 7 mm or less, and the total flow sectional area St is 2.5 mm ² or more. The liquid processing nozzle according to claim 3, which is set to 35 mm ² or less.
6. The liquid processing nozzle according to claim 5, wherein a liquid circulation gap is formed at a center position of a cross formed by the four collision portions, and the 70% cross-sectional ratio σ ₇₀ is secured by 40% or more.
7. 2. The gas injection hole that opens on the outer peripheral surface of the nozzle main body and communicates with the processing core portion upstream of at least one of the plurality of collision portions is formed in the nozzle main body. The liquid processing nozzle according to claim 6.
8. A partition that partitions the liquid channel into an inflow chamber on the liquid inlet side and an outflow chamber on the liquid outlet side, and a plurality of passages that are formed through the partition and communicate with the inflow chamber and the outflow chamber through different paths. The liquid processing nozzle according to claim 1, wherein the collision portion is formed so as to protrude from an inner surface of the throttle hole. .
9. The throttle hole has a throttle hole aspect ratio defined by L / de of 3.5 or less, where de is the diameter of a circle equivalent to the sum of the axial cross-sectional areas of the throttle holes, and L is the length of the throttle hole. In the projection onto the plane perpendicular to the axis of the nozzle body, the distance from the reference point determined at the center position of the projection area of the partition wall to the inner peripheral edges of the plurality of aperture holes The liquid processing nozzle according to claim 8, wherein the liquid processing nozzles are arranged close to each other so that T is smaller than an inner diameter d of the throttle hole.
10. 10. A liquid treatment comprising: supplying a liquid to the liquid inlet of the liquid treatment nozzle according to claim 1; and bringing the liquid into contact with the impinging portion and flowing out from the liquid outlet. Method.
11. The liquid processing method according to claim 10, wherein the liquid is water in which a gas is dissolved, and the liquid is discharged as fine bubble-containing water containing fine bubbles derived from the gas dissolved from the liquid outlet.
12. The liquid treatment nozzle is provided in the toilet toilet wash water supply pipe, and the wash water in the pipe is supplied to the toilet after the liquid treatment nozzle makes the fine bubble-containing water, The liquid processing method of Claim 11 which wash | cleans the inside of the waste water drain pipe of a toilet bowl.
13. 10. The liquid processing nozzle according to claim 1, wherein a mixed phase flow of a liquid and a gas is supplied to the collision portion of the liquid processing nozzle so that the gas is dissolved in the liquid and flows out from the liquid outlet. A gas melting method characterized by comprising:
14. The gas dissolving method according to claim 13, wherein the liquid is water and the gas is carbon dioxide.
15. The gas dissolving method according to claim 13, wherein the liquid is water and the gas is nitrogen.
16. The gas dissolving method according to claim 13, wherein the liquid is water and the gas is oxygen.
17. A liquid processing nozzle according to any one of claims 1 to 9, and a multiphase flow supply means for supplying a multiphase flow of a liquid and a gas to the collision portion of the liquid processing nozzle, A gas dissolving apparatus characterized in that a gas is dissolved from the liquid and flows out from the liquid outlet.
18. The multiphase flow supply means supplies a multiphase flow of water and carbon dioxide gas,
    18. The gas dissolving device according to claim 17, further comprising a sodium hypochlorite aqueous solution supply unit that quantitatively supplies a sodium hypochlorite aqueous solution to the water in which the carbon dioxide gas delivered from the liquid processing nozzle is dissolved.

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